CN113072970A - System and method for preparing bio-oil by pyrolysis coupling fractional condensation - Google Patents
System and method for preparing bio-oil by pyrolysis coupling fractional condensation Download PDFInfo
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- CN113072970A CN113072970A CN202110417172.9A CN202110417172A CN113072970A CN 113072970 A CN113072970 A CN 113072970A CN 202110417172 A CN202110417172 A CN 202110417172A CN 113072970 A CN113072970 A CN 113072970A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G5/00—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas
- C10G5/06—Recovery of liquid hydrocarbon mixtures from gases, e.g. natural gas by cooling or compressing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
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Abstract
本发明公开了一种热解耦合分级冷凝制备生物油的系统，包括炭粉燃烧炉、流化床热解反应器、气固分离装置和分级冷凝装置，炭粉燃烧炉与流化床热解反应器连通，通过风机将炭粉燃烧炉中燃烧炭粉产生的高温烟气输送至流化床热解反应器，提供生物质料发生热解反应的热能；气固分离装置与流化床热解反应器连通，气固分离装置用于将流化床热解反应器排出的气固混合物分离成炭粉和热解气；分级冷凝装置与气固分离装置连接，分级冷凝装置用于将热解气分级冷凝成生物油。炭粉燃烧炉的燃烧副产物‑炭粉即可满足流化床反应器的需求，不需要额外的能源投入，降低了生产成本，并且通过分级冷凝获得了种类更丰富的生物油。本发明还公开了一种制备生物油的方法。
The invention discloses a system for preparing bio-oil by pyrolysis coupled with graded condensation. The reactor is connected, and the high-temperature flue gas generated by burning the carbon powder in the carbon powder combustion furnace is transported to the fluidized bed pyrolysis reactor through the fan to provide the thermal energy for the pyrolysis reaction of the biomass material; the gas-solid separation device is connected to the fluidized bed pyrolysis reactor. The reactor is connected, and the gas-solid separation device is used to separate the gas-solid mixture discharged from the fluidized bed pyrolysis reactor into carbon powder and pyrolysis gas; the grading condensation device is connected with the gas-solid separation device, and the grading condensation device is used for pyrolysis. The gas is staged and condensed into bio-oil. The combustion by-products of the pulverized carbon burner—the pulverized carbon can meet the needs of the fluidized bed reactor, which does not require additional energy input, reduces the production cost, and obtains a richer variety of bio-oils through staged condensation. The invention also discloses a method for preparing biological oil.
Description
Technical Field
The invention relates to the technical field of biomass regeneration, utilization and energy regeneration equipment, in particular to a system and a method for preparing bio-oil by pyrolysis coupling fractional condensation.
Background
The biomass pyrolysis liquefaction technology is a technological process for obtaining liquid product bio-oil by rapidly heating and decomposing lignocellulose biomass (hereinafter referred to as biomass) such as agricultural and forestry waste under the anaerobic or anoxic condition and quenching separated pyrolysis gas. Compared with biological raw materials, the biological oil has large volumetric energy density, so the biological oil has high collection, transportation and storage effects, rich high value-added components and high comprehensive utilization value. The existing biomass pyrolysis liquefaction equipment for experiments at home and abroad mostly adopts an electric heating type pyrolysis reactor, although the heating rate and the pyrolysis temperature are easy to control, the electric heating energy consumption is large, the cost is high, and therefore, the corresponding equipment and technology are difficult to be industrially amplified to adapt to large-scale production. The existing commercial Biomass pyrolysis liquefaction technology and equipment scale of each country are greatly different, for example, the maximum treatment capacity of a fluidized bed Biomass pyrolysis liquefaction device of British Biomass engineering Ltd is 200kg/h, the maximum treatment capacity of a moving bed pyrolysis liquefaction device of Ensyn in Canada can reach 500kg/h, and the maximum treatment capacity of a rotating cone pyrolysis liquefaction device of BTG in the Netherlands can also reach 500 kg/h. However, most of the existing commercial pyrolysis liquefaction equipment adopts high-price liquefied petroleum gas or natural gas to provide a heat source for the pyrolysis reaction, and the consumption is large, so that the production cost of the bio-oil is high. Although the production cost of bio-oil is lower as the biomass treatment efficiency is improved, the economic benefit analysis performed by the existing biomass pyrolysis liquefaction process shows that the production cost of bio-oil of the existing commercial pyrolysis liquefaction device cannot be lower than 5000 yuan/ton even if the biomass treatment capacity reaches 1000 tons/day. Therefore, under the large background that the international oil price is continuously lowered, from the viewpoint of reducing the production cost of the bio-oil, research and development of a new technology and a new method which do not need to consume high-grade energy sources such as high-price electric energy and provide heat sources for pyrolysis are carried out, and the key to whether the biomass pyrolysis liquefaction technology can be popularized and applied in a large scale is provided.
In addition, the bio-oil collected by the traditional condensing means used by the existing commercial devices for biomass pyrolysis liquefaction at home and abroad usually has the defects of single quality of bio-oil, excessively complex components and the like, so that the difficulty of subsequent development and utilization of the bio-oil, such as refining, separation and purification, is quite high, the exertion of the comprehensive utilization value of the bio-oil is seriously influenced, and the development and application of the biomass pyrolysis liquefaction technology are also restricted.
Disclosure of Invention
In order to solve the technical problem, the invention discloses a system for preparing bio-oil by pyrolysis coupling fractional condensation, which can utilize byproducts as fuel to provide heat energy, thereby greatly reducing the cost of biomass pyrolysis liquefaction.
The invention discloses a system for preparing bio-oil by pyrolysis coupling fractional condensation, which comprises: a powdered carbon combustion furnace, a fluidized bed pyrolysis reactor, a gas-solid separation device and a fractional condensation device, wherein,
the carbon powder combustion furnace is communicated with the fluidized bed pyrolysis reactor and is used for conveying the combusted flue gas to the fluidized bed pyrolysis reactor so that the flue gas can generate pyrolysis reaction after supplying heat energy to the biomass material in the fluidized bed pyrolysis reactor;
the gas-solid separation device is communicated with the fluidized bed pyrolysis reactor and is used for separating a gas-solid mixture discharged from the fluidized bed pyrolysis reactor into carbon powder and pyrolysis gas, and the carbon powder is used as a fuel of the carbon powder combustion furnace;
the grading condensing device is connected with the gas-solid separation device and is used for grading and condensing the pyrolysis gas into the bio-oil.
According to some embodiments of the invention, the system for preparing bio-oil by pyrolysis coupled fractional condensation further comprises:
the tail gas combustion device is communicated with the fractional condensation device and is used for combusting tail gas discharged by the fractional condensation device, and the tail gas combustion device is used for introducing combusted gas into the heat-insulation jacket;
wherein the heat-preservation jacket is arranged outside the carbon powder combustion furnace, the fluidized bed pyrolysis reactor, the gas-solid separation device, the fractional condensation device and the pipeline therebetween.
According to some embodiments of the invention, the system for preparing bio-oil by pyrolysis coupled fractional condensation further comprises:
the carbon powder feeding device is communicated with the carbon powder combustion furnace and is used for conveying carbon powder into the carbon powder combustion furnace;
the biomass feeding device is communicated with the fluidized bed pyrolysis reactor and is used for conveying a biomass material to the fluidized bed pyrolysis reactor so that the biomass material and the flue gas are mixed and then subjected to pyrolysis reaction.
According to some embodiments of the present invention, the fluidized bed pyrolysis reactor includes a cylindrical fluidized bed pyrolysis furnace, an air inlet is disposed at a bottom of the fluidized bed pyrolysis furnace, the air inlet is communicated with a flue gas outlet of the carbon powder combustion furnace, a biomass feed port and an air outlet are disposed at a top of the fluidized bed pyrolysis furnace, the biomass feed port is communicated with a biomass feed device, and the air outlet is used for discharging a gas-solid mixture obtained after pyrolysis of the biomass material, wherein the gas-solid mixture includes carbon powder and pyrolysis gas.
According to some embodiments of the invention, the gas-solid separation device comprises at least one cyclone separator, an ash bucket of the cyclone separator is communicated with the carbon powder storage tank, and a plurality of cyclone separators are connected in sequence.
According to some embodiments of the invention, the fractional condensation device comprises a first condenser, the first condenser comprises a spraying condensation section, a first liquid cooling condensation section and a first liquid storage section from top to bottom, the top of the first condenser is provided with a first condenser air inlet and a spraying port, the first condenser air inlet is communicated with the gas-solid separation device, the spraying port can spray a spraying medium, the first liquid cooling condensation section comprises a first tubular heat exchanger, cooling liquid flows in the first tubular heat exchanger in a circulating manner, the first liquid storage section stores the spraying medium and bio-oil obtained by condensation, and a first condenser air outlet is arranged above the first liquid storage section.
According to some embodiments of the invention, the fractional condensation device comprises at least one second condenser, the second condenser comprises a second liquid cooling condensation section, a filling section and a second liquid storage section from top to bottom, the second liquid cooling condensation section comprises a second tubular heat exchanger, cooling liquid circulates in the second tubular heat exchanger, the filling section is used for filling a filling material, the second liquid storage section is used for storing condensed liquid, and a plurality of second condensers are connected in sequence.
The invention also discloses a method for preparing the bio-oil by pyrolysis coupling fractional condensation by using the system for preparing the bio-oil by pyrolysis coupling fractional condensation, which comprises the following steps:
conveying the carbon powder to a carbon powder combustion furnace for combustion, and introducing the combusted flue gas into a fluidized bed pyrolysis reactor;
conveying a biomass material into the fluidized bed pyrolysis reactor, and mixing the biomass material with the flue gas to perform pyrolysis reaction;
separating the mixed gas output by the fluidized bed pyrolysis reactor into carbon powder and pyrolysis gas by using a gas-solid separation device, and collecting the carbon powder into a carbon powder storage tank;
and carrying out fractional condensation on the pyrolysis gas into the bio-oil through a fractional condensation device.
According to some embodiments of the present invention, the tail gas discharged from the fractional condensation device is combusted by a tail gas combustion device, and the gas obtained after the combustion is introduced into a heat-insulating jacket, wherein the heat-insulating jacket is disposed outside the combustion furnace, the fluidized bed pyrolysis reactor, the gas-solid separation device, the fractional condensation device and a pipeline therebetween.
According to some embodiments of the invention, the temperature of the flue gas ranges from 500 ℃ to 650 ℃, the temperature of the pyrolysis gas ranges from 250 ℃ to 350 ℃, and the temperature of the tail gas discharged from the fractional condensation device ranges from 20 ℃ to 30 ℃.
According to the technical scheme, high-temperature flue gas is provided for the fluidized bed pyrolysis reactor by the carbon powder combustion furnace, the high-temperature flue gas is mixed with granular biomass materials and then subjected to pyrolysis reaction to generate multi-component mixed pyrolysis gas of gaseous bio-oil, carbon monoxide and the like and solid residue carbon powder of the biomass materials, the carbon powder is separated by the gas-solid separation device and can be combusted in the carbon powder combustion furnace after being recovered, and the bio-oil is obtained by condensing the pyrolysis gas in a grading manner by the grading condensation device. According to the technical scheme disclosed by the invention, the pyrolysis reactor does not need to consume extra energy, the by-product (carbon powder) can meet the requirement of a carbon powder combustion furnace, the production cost of the bio-oil is greatly reduced, meanwhile, the bio-oil obtained by fractional condensation is rich in variety and high in component enrichment degree, and can be adjusted according to actual needs.
Drawings
FIG. 1 is a schematic diagram showing the structure of a system for preparing bio-oil by pyrolysis coupling fractional condensation according to an embodiment of the invention;
FIG. 2 is a schematic diagram illustrating a carbon powder combustion furnace and a carbon powder feeding device of a system for preparing bio-oil by pyrolysis coupling fractional condensation according to an embodiment of the present invention;
FIG. 3 is a schematic diagram showing the structure of a fluidized bed pyrolysis reactor and a gas-solid separation device of a system for preparing bio-oil by pyrolysis coupling fractional condensation according to an embodiment of the present invention;
FIG. 4 is a schematic diagram illustrating the structure of a system for preparing bio-oil by pyrolysis-coupled fractional condensation according to an embodiment of the present invention;
FIG. 5 is a schematic diagram showing the structure of a fractional condensation device of a system for preparing bio-oil by pyrolysis coupling fractional condensation according to an embodiment of the invention;
FIG. 6 schematically illustrates a flow diagram of a method for preparing bio-oil by pyrolysis-coupled fractional condensation according to an embodiment of the present invention;
FIG. 7 is a schematic diagram showing the structure of a system for preparing bio-oil by pyrolysis-coupled fractional condensation according to another embodiment of the present invention;
in the above figures, the reference numerals have the following meanings:
100-charcoal powder combustion furnace;
200-a fluidized bed pyrolysis reactor;
300-a gas-solid separation device;
400-fractional condensation unit;
500-a tail gas combustion device;
600-heat preservation jacket;
700-carbon powder feeding device;
800-a biomass feed device;
900-bio-oil;
101-carbon powder feed port; 102-a flue gas outlet; 103-air inlet of carbon powder combustion furnace; 104-a blower device;
201-a pyrolysis reaction chamber; 202-an air inlet; 203-blanking pipe; 204-biomass feed inlet; 205-gas outlet;
301-cyclone outlet; 302-cyclone inlet; 303-cyclone separator chamber; 304-ash bucket; 305-charcoal powder storage bin;
401-a first condenser; 4011-spray condensation section; 4012-a spray port; 4013 — a first liquid-cooled condensation section; 4014-first stock solution stage; 4015-reflux unit;
402-a second condenser; 4021-a second liquid cooling and condensing section; 4022-a filler section; 4023-a second stock solution;
701-a first feedwell; 702-a first screw feeder;
801-a second feedwell; 802-second screw feeder.
Detailed Description
In order that the objects, technical solutions and advantages of the present invention will become more apparent, the present invention will be further described in detail with reference to the accompanying drawings in conjunction with the following specific embodiments.
It is to be understood that such description is merely illustrative and not intended to limit the scope of the present invention. In the following detailed description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the embodiments of the invention. It may be evident, however, that one or more embodiments may be practiced without these specific details. Furthermore, in the following description, descriptions of well-known technologies are omitted so as to avoid unnecessarily obscuring the concepts of the present invention.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the invention. The term "comprising" as used herein indicates the presence of the features, steps, operations but does not preclude the presence or addition of one or more other features.
All terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art unless otherwise defined. It is noted that the terms used herein should be interpreted as having a meaning that is consistent with the context of this specification and should not be interpreted in an idealized or overly formal sense.
In order to solve the technical problems, the invention discloses a system for preparing bio-oil by pyrolysis coupling fractional condensation, which can utilize a byproduct (carbon powder) as a fuel to provide heat energy, thereby greatly reducing the cost of biomass pyrolysis liquefaction.
Fig. 1 schematically shows a schematic structural diagram of a system for preparing bio-oil by pyrolysis coupling according to an embodiment of the present invention.
The invention discloses a system for preparing bio-oil by pyrolysis coupling, as shown in figure 1, the system comprises: the system comprises a carbon powder combustion furnace 100, a fluidized bed pyrolysis reactor 200, a gas-solid separation device 300 and a fractional condensation device 400.
Fig. 2 is a schematic diagram illustrating a carbon powder combustion furnace and a carbon powder feeding device of a system for preparing bio-oil by pyrolysis coupling fractional condensation according to an embodiment of the present invention.
According to some embodiments of the present invention, as shown in fig. 2, the carbon powder combustion furnace 100 includes a combustion chamber, a carbon powder feed port 101 and a flue gas outlet 102, wherein carbon powder is fed from the carbon powder feed port 101 to the combustion chamber for combustion, it should be noted that oxygen-enriched combustion should be avoided during combustion of carbon powder.
According to some embodiments of the present invention, the soot of the carbon powder after combustion in the combustion chamber is transferred from the flue gas outlet 102 to the fluidized bed pyrolysis reactor 200, wherein the temperature of the flue gas is controlled to be maintained in the range of 500 ℃ to 650 ℃.
According to some embodiments of the present invention, as shown in fig. 2, the bottom of the carbon powder combustion furnace 100 is provided with a carbon powder combustion furnace air inlet 103, and further includes a blower 104 connected to the carbon powder combustion furnace air inlet 103, wherein the blower 104 introduces air into the combustion chamber through a blower to control the combustion process of the carbon powder.
According to some embodiments of the invention, the blower is a roots blower.
According to some embodiments of the present invention, the carbon powder combustion furnace 100 is in communication with the fluidized bed pyrolysis reactor 200, and the carbon powder combustion furnace 100 is configured to deliver the combusted flue gas to the fluidized bed pyrolysis reactor 200, so that the flue gas and the biomass material in the fluidized bed pyrolysis reactor 200 undergo a pyrolysis reaction.
According to some embodiments of the present invention, the inner diameter of the carbon powder combustion furnace 100 ranges from 350mm to 450mm, the effective height ranges from 800mm to 900mm, the combustion effect of the carbon powder is good, and the generated smoke is good.
Fig. 3 is a schematic diagram illustrating the structure of a fluidized bed pyrolysis reactor and a gas-solid separation device of a system for preparing bio-oil by pyrolysis coupled fractional condensation according to an embodiment of the present invention.
According to some embodiments of the present invention, as shown in fig. 3, the fluidized bed pyrolysis reactor 200 includes a columnar fluidized bed pyrolysis furnace, a pyrolysis reaction chamber 201 is disposed in the fluidized bed pyrolysis furnace, an air inlet 202 is disposed at a bottom of the flow pyrolysis reaction chamber 201, the air inlet 202 is communicated with the bright gas outlet 102 of the carbon powder combustion furnace 100, a biomass feed port 204 and an air outlet 205 are disposed at a top of the fluidized bed pyrolysis furnace, the biomass feed port 204 is communicated with a biomass feed device 800, and the air outlet 205 is used for discharging a gas-solid mixture obtained after pyrolysis of a biomass material, where the gas-solid mixture includes carbon powder and pyrolysis gas.
According to some embodiments of the invention, the effective height of the fluidized bed pyrolysis reactor is 2500 mm-3000 mm, the inner diameters are equal or different from bottom to top, the value range of the inner diameters is 240 mm-280 mm, and the pyrolysis liquefaction reaction efficiency of the biomass material is high.
According to some embodiments of the present invention, the biomass material enters the pyrolysis reaction chamber 201 from the biomass inlet 204, falls into the bottom from the top of the pyrolysis reaction chamber 201, and meanwhile, the high temperature flue gas enters from the bottom of the pyrolysis reaction chamber 201, after the biomass material and the high temperature flue gas generate strong momentum and heat exchange, the biomass material is carried by the high temperature flue gas to flow upward and undergo pyrolysis, the biomass material separates out pyrolysis gas and carbon powder, and then the mixed gas flow composed of the flue gas, the carbon powder and the pyrolysis gas is carried by the mixed gas flow to flow upward, and flows out of the fluidized bed type pyrolysis reactor 200 through the gas outlet 205 at the top of the pyrolysis reaction chamber 201, so as to complete the pyrolysis process.
According to some embodiments of the present invention, a blanking pipe 203 is disposed in the fluidized bed type pyrolysis reactor 200, and one end of the blanking pipe 203 is communicated with the biomass feed inlet 204, and the other end is located inside the pyrolysis reaction chamber 201. Optionally, the other end of the feeding hole 204 is located in the middle or the upper portion of the pyrolysis reaction cavity 201 to increase the contact time between the biomass material and the flue gas, so as to prevent the biomass material from undergoing no pyrolysis reaction or incomplete pyrolysis liquefaction reaction.
According to some embodiments of the present invention, the ratio of the amount of air supplied by the blower 104 into the combustion chamber to the biomass material delivered into the fluidized bed pyrolysis reactor 200 is: air intake (m) of combustion furnace3The feed rate of the pyrolysis biomass (kg/h) is 1.0-1.5.
Fig. 4 is a schematic structural diagram of a system for preparing bio-oil by pyrolysis coupling according to another embodiment of the present invention.
According to some embodiments of the present invention, as shown in fig. 4, the system for preparing bio-oil by pyrolysis coupling further comprises: carbon powder feed device 700 and biomass feed device 800.
According to some embodiments of the present invention, as shown in fig. 2, a carbon powder feeding device 700 comprises a first feeding barrel 701 and a first screw feeding device 702, carbon powder is fed into the first feeding barrel 701 and is conveyed to the carbon powder combustion furnace 100 by the first screw feeding device 702 according to a preset amount for combustion.
According to some embodiments of the present invention, as shown in fig. 3, the biomass feeding device 800 includes a second feeding barrel 801 and a second screw feeding device 802, and the biomass material is fed into the second feeding barrel 801 and is transferred into the fluidized bed pyrolysis reactor 200 by the second screw feeding device 802 in a preset amount to participate in the pyrolysis liquefaction reaction.
According to some embodiments of the invention, the biomass material is granular, which can increase the contact area with the high-temperature flue gas, and accelerate the pyrolysis liquefaction reaction and the generation speed of the carbon powder.
According to some embodiments of the present invention, as shown in fig. 3 and 4, a gas-solid separating device 300 is in communication with the fluidized-bed pyrolysis reactor 200, and the gas-solid separating device 300 is used to separate a gas-solid mixture discharged from the fluidized-bed pyrolysis reactor 200 into carbon powder as fuel of a carbon powder combustion furnace and pyrolysis gas.
According to some embodiments of the present invention, the gas-solid separation device 300 comprises at least one cyclone, the ash hopper 304 of which is connected to the carbon powder storage tank 305, wherein a plurality of cyclones are connected in sequence.
According to some embodiments of the present invention, the mixed gas stream enters the cyclone inlet 302, is separated out in the cyclone chamber 303, and the carbon powder enters the carbon powder storage tank 305 through the cyclone chamber 303 and the ash hopper 304.
According to some embodiments of the present invention, the outlet of the previous cyclone is communicated with the inlet of the next cyclone, and the carbon powder in the mixed gas flow is separated by a plurality of cyclones connected in series, so as to improve the separation rate of the carbon powder.
According to some embodiments of the present invention, a fractional condensation device 400 is connected to the gas-solid separation device 300, and the fractional condensation device 400 is used for fractional condensation of pyrolysis gas into bio-oil 900.
FIG. 5 is a schematic diagram showing the structure of a fractional condensation device of a system for preparing bio-oil by pyrolysis coupling fractional condensation according to an embodiment of the invention.
According to some embodiments of the present invention, as shown in fig. 5, the staged condensation device 400 includes a first condenser 401, the first condenser 401 includes, from top to bottom, a spray condensation section 4011, a first liquid-cooled condensation section 4013, and a first liquid storage section 4014, a first condenser air inlet and a spray port 4012 are disposed at a top of the first condenser 401, the first condenser air inlet is communicated with the gas-solid separation device 400, the spray port 4012 can spray a spray medium, the first liquid-cooled condensation section 4013 includes a first tubular heat exchanger in which a coolant circulates, the first liquid storage section 4014 stores the spray medium and bio-oil 900 obtained by condensation, and a first condenser air outlet is disposed above the first liquid storage section 4014.
According to some embodiments of the present invention, the spraying medium sprayed from the spraying port 4012 is an alcohol organic solvent or bio-oil 900 obtained by pyrolysis.
Optionally, at the initial stage of system operation, an alcohol organic solvent is used as a spraying medium to condense the pyrolysis gas.
According to some embodiments of the invention, the first condenser 401 comprises a backflow device 4015, and two ends of the backflow device 4015 are respectively connected with the spray port 4012 and the first stock solution section 4014. After the first reservoir segment 4014 stores part of the bio-oil 900, the bio-oil 900 in the first reservoir segment 4014 is delivered to the spray port 4012 by the reflux pump and sprayed out.
According to some embodiments of the present invention, the pyrolysis gas introduced from the gas inlet of the first condenser enters the first condenser 401, and then contacts with the spraying medium to obtain rapid cooling, wherein a part of condensable components are condensed into liquid, the rest of the pyrolysis gas still remaining in a gaseous state enters the first liquid cooling condensation section 4013, the spraying medium from the upper portion, the liquid (bio-oil) obtained by condensation, the fluidization carrier gas, and the uncondensed pyrolysis gas undergo partition wall heat exchange with the circulating cooling water in the tubes when flowing through the tube wall of the tubes to obtain further cooling, a part of the pyrolysis gas which has not been condensed before is condensed into liquid, and flows into the first liquid storage section 4014, and the rest of the fluidization carrier gas and the uncondensed pyrolysis gas are conveyed to the second condenser 402 through the gas outlet of the first condenser to be further condensed.
According to some embodiments of the present invention, the effective height of the spray condensing section 4011 is 800mm to 1000mm, the effective height of the first liquid-cooled condensing section 4013 is 900mm to 1100mm, and the effective height of the first liquid reservoir section 4014 is 800mm to 1000 mm. The size of the first condenser 401 is adaptively adjusted according to the composition or kind of bio-oil required.
According to some embodiments of the present invention, the fractional condensation device 400 includes at least one second condenser 402, the second condenser 402 includes a second liquid cooling condensation section 4021, a filling section 4022 and a second liquid storage section 4023 from top to bottom, the second liquid cooling condensation section 4021 includes a second tubular heat exchanger, a cooling liquid circulates in the second tubular heat exchanger, the filling section 4022 is used for filling a filling material, the second liquid storage section 4023 is used for storing a condensed liquid, and the plurality of second condensers 402 are connected in sequence.
According to some embodiments of the invention, after the fluidizing carrier gas and uncondensed pyrolysis gas from the upper-stage condenser enter the current-stage condenser from the gas inlet above the liquid storage section, the fluidizing carrier gas and uncondensed pyrolysis gas flow upwards through the packing section and are subjected to partition-wall heat exchange with circulating cooling water in the tubular heat exchanger to obtain further cooling, the condensable pyrolysis gas which is not condensed before is partially condensed into liquid, and the condensate flows downwards under the action of gravity.
According to some embodiments of the present invention, the condensate flowing downward from second condenser 402 is momentum and heat exchanged with the upward flowing gas stream as it passes through packing section 4022, and thus packing section 4022 also functions to cool and condense.
According to some embodiments of the invention, the packing section 4022 is filled with packing, the pyrolysis gas moves upward through gaps between the packing, and the packing acts as a carrier for condensation to condense the condensable pyrolysis gas into liquid, which improves the efficiency of condensing the bio-oil 900.
According to some embodiments of the invention, in the process of fractional cooling and condensation of the pyrolysis gas, the condensation temperature of each stage of condenser is mainly controlled by adjusting the temperature and flow of the circulating cooling water of each stage of condenser, so that the bio-oil with high enrichment of various components is separated.
According to some embodiments of the invention, the effective height of the second liquid cold condensation section 4021 is 800mm to 1000mm, the effective height of the filler section 4022 is 900mm to 1100mm, and the effective height of the second liquid storage section 4023 is 800mm to 1000 mm. The size of the second condenser 402 is adaptively adjusted according to the composition or kind of bio-oil required.
According to some embodiments of the invention, the system for preparing bio-oil by pyrolysis coupled fractional condensation further comprises: tail gas combustion device 500 and heat preservation jacket 600.
According to some embodiments of the present invention, the exhaust gas combustion device 500 is connected to a negative pressure circulation device, and the gas generated by the reaction of the exhaust gas combustion device 500 is transported to the thermal insulation jacket 600 through the negative pressure circulation device.
According to some embodiments of the present invention, the tail gas combustion device 500 is communicated with the staged condensation device 400, the tail gas combustion device 500 is used for combusting the tail gas discharged from the staged condensation device 400, and the tail gas combustion device 500 is used for introducing the combusted gas into the heat-insulating jacket 600.
According to some embodiments of the present invention, after condensation by the multi-stage condenser, the condensable portion of the pyrolysis gas is substantially completely condensed into bio-oil, the tail gas discharged from the last condenser includes carbon dioxide, carbon monoxide, methane, hydrogen, etc., and after being processed by the tail gas combustion device 500, the processed high temperature gas is delivered into the thermal insulation jacket 600 to achieve thermal insulation of the devices in the thermal insulation jacket 600.
According to some embodiments of the present invention, the heat-insulating jacket 600 is provided with an inner cavity, and the gas treated by the tail gas combustion device 500 is discharged after passing through the inner cavity of the heat-insulating jacket 600, so that energy is fully utilized, and environmental pollution is reduced.
According to some embodiments of the present invention, at least one of the charcoal powder burner 100, the fluidized-bed pyrolysis reactor 200, the gas-solid separation device 300, and the fractional condensation device 400 is externally provided with a heat-insulating jacket 600.
FIG. 6 schematically shows a flow chart of a method for preparing bio-oil by pyrolysis coupling according to an embodiment of the present invention.
The invention also discloses a method for preparing bio-oil by pyrolysis coupling by using the system for preparing bio-oil by pyrolysis coupling, as shown in fig. 6, the method comprises steps S1 to S4.
According to some embodiments of the invention, step S1 includes: the carbon powder is transported to the carbon powder combustion furnace 100 for combustion, and the combusted flue gas is introduced into the fluidized bed pyrolysis reactor 200.
According to some embodiments of the invention, step S2 includes: the biomass material is transported into the fluidized bed pyrolysis reactor 200, and the biomass material and the flue gas are mixed to generate a pyrolysis reaction.
According to some embodiments of the invention, step S3 includes: the gas-solid mixture output from the fluidized bed pyrolysis reactor 200 is separated into carbon powder and pyrolysis gas by the gas-solid separation device 300, and the carbon powder is collected into the carbon powder storage tank 305.
According to some embodiments of the invention, step S4 includes: the pyrolysis gas is condensed into bio-oil 900 by stages through a fractional condensation device 400.
According to some embodiments of the present invention, the tail gas discharged from the fractional condensation device 400 is combusted by the tail gas combustion device 500, and the gas obtained after the combustion is introduced into the heat-insulating jacket 600, wherein the heat-insulating jacket 600 is disposed outside at least one of the carbon powder combustion furnace 100, the fluidized bed pyrolysis reactor 200, the gas-solid separation device 300, and the fractional condensation device 400.
According to some embodiments of the invention, the temperature of the flue gas ranges from 500 ℃ to 650 ℃, the temperature of the pyrolysis gas ranges from 250 ℃ to 350 ℃, and the temperature of the tail gas discharged from the fractional condensation device ranges from 20 ℃ to 30 ℃.
According to some embodiments of the invention, the working temperature of each process of the system is controlled to realize fractional cooling and condensation of the pyrolysis gas to obtain the bio-oil with different components.
According to some embodiments of the present invention, the temperature of the flue gas is controlled to be 500 to 650 ℃ by controlling the flow rate of the air introduced into the carbon powder combustion furnace 100, and the temperature of the pyrolysis gas separated by the gas-solid separation device 300 is controlled to be about 300 ℃, that is, the temperature of the pyrolysis gas introduced into the inlet of the first condenser 401 is 300 ℃, the temperature of the bio-oil 900 stored in the first liquid storage section 4014 is 70 to 100 ℃, the temperature of the pyrolysis gas introduced into the second condenser 401 of the first stage is controlled to be 60 to 80 ℃, and the temperature of the pyrolysis gas introduced into the second condenser 401 of the second stage is 20 to 30 ℃. The temperature of the gas-solid separation device 300 is controlled by the heat-insulating jacket 600.
The technical solutions disclosed in the present invention are further described below with reference to specific examples, and it should be understood that the specific examples are only for helping those skilled in the art to better understand the technical solutions of the present invention, and are not intended to limit the scope of the present invention.
The first embodiment is as follows:
as shown in fig. 2, the fluidized bed pyrolysis reactor 200 has an effective height of 2800mm and an equal inside diameter from bottom to top, which is 260 mm; the inner diameter of the carbon powder combustion furnace 100 is 410mm, and the effective height is 850 mm; the fractional condensation device 400 comprises a first condenser 401 and two second condensers 402, the inner diameters of the first condenser 401 and the second condensers 402 are both 410mm, wherein: the effective height of the spraying condensation section 4011 is 900mm, the effective height of the first liquid cooling condensation section 4013 is 1000mm, and the effective height of the first liquid storage section 4014 is 900 mm; the effective heights of the second liquid cooling condensation sections 4021 of the two second condensers 402 are both 900mm, the effective heights of the filler sections 4022 are both 1000mm, and the effective heights of the lower liquid storage sections are both 900 mm.
The rice hulls are used as the biomass material to prepare the bio-oil through pyrolysis and liquefaction, and the test of preparing the bio-oil through pyrolysis is carried out for many times, and the obtained results are as follows:
(1) the pyrolysis treatment capacity of the system during stable operation is 200kg/h, the total yield of the bio-oil is 51.2%, wherein the proportion of the bio-oil collected by the first-stage cooling and condensing device in the total bio-oil is 68%, the proportion of the second-stage cooling and condensing device in the total bio-oil is 23%, and the proportion of the third-stage cooling and condensing device in the total bio-oil is 9%.
(2) The yield and the heat value of the carbon powder are respectively 60kg/h and 24MJ/kg when the device is in stable operation, and the yield and the heat value of the non-condensable combustible gas are respectively 40m3H and 12MJ/m3。
(3) The burning rate of the carbon powder is 40kg/h when the device is in stable operation.
Based on the test results, the yield of the byproduct, namely the carbon powder, is greater than the consumption of the carbon powder when the system operates stably, and based on the method and the system, the pyrolysis of the biomass material can be completed without additional consumption of energy (such as fossil fuel or electric energy), so that the production cost is reduced.
Example two:
fig. 7 is a schematic structural diagram of a system for preparing bio-oil by pyrolysis coupling according to another embodiment of the present invention, and as shown in fig. 7, an effective height of a fluidized bed pyrolysis reactor 200 is 2500mm, which is divided into two sections from bottom to top: the upper part is an equal-diameter section with the inner diameter of 410mm, the lower part is a variable-diameter section with the inner diameter of 410mm at the upper end and the inner diameter of 260mm at the lower end; the inner diameter of the carbon powder combustion furnace 100 is 410mm, and the effective height is 850 mm; the fractional condensation device 400 comprises a first condenser 401 and two second condensers 402, the inner diameters of the first condenser 401 and the second condensers 402 are both 410mm, wherein: the effective height of the spraying condensation section 4011 is 900mm, the effective height of the first liquid cooling condensation section 4013 is 1000mm, and the effective height of the first liquid storage section 4014 is 900 mm; the effective heights of the second liquid cooling condensation sections 4021 of the two second condensers 402 are both 900mm, the effective heights of the filler sections 4022 are both 1000mm, and the effective heights of the lower liquid storage sections are both 900 mm.
The rice hulls are used as the biomass material to prepare the bio-oil through pyrolysis and liquefaction, and the test of preparing the bio-oil through pyrolysis is carried out for many times, and the obtained results are as follows:
(1) the pyrolysis treatment capacity of the device during stable operation is 500kg/h, the total yield of the bio-oil is 51.5%, wherein the proportion of the bio-oil collected by the first-stage cooling and condensing device in the total bio-oil is 68%, the proportion of the second-stage cooling and condensing device in the total bio-oil is 23%, and the proportion of the third-stage cooling and condensing device in the total bio-oil is 9%.
(2) The yield and the heat value of the carbon powder are respectively 150kg/h and 24MJ/kg when the device is in stable operation, and the yield and the heat value of the non-condensable combustible gas are respectively 100m3H and 12MJ/m3。
(3) The burning rate of the carbon powder is 100kg/h when the device is in stable operation.
According to the test results, the yield of the byproduct, namely the carbon powder, is also higher than the consumption of the carbon powder when the system is in stable operation, and the pyrolysis treatment capacity is improved to 500kg/h compared with 200kg/h in the first embodiment.
For example, in the conventional biomass pyrolysis liquefaction apparatus, the electric heating power of a commercial apparatus with a pyrolysis processing capacity of 1000kg/h is at least 200kW or more, 400kWh is consumed for each 1 ton of bio-oil production (assuming that the bio-oil yield is 50% for convenience estimation), and if the electricity fee is calculated as 0.8 yuan/kWh, the cost of only electrically heating for each 1 ton of bio-oil production reaches 320 yuan/ton. The invention adopts combustion of partial carbon powder to provide a heat source for pyrolysis, and a commercial device with the same pyrolysis scale (1000kg/h) needs to burn 120kg of carbon powder for producing 1 ton of bio-oil, and if the carbon powder is calculated according to 500 yuan/ton, the heating cost for producing 1 ton of bio-oil only needs 60 yuan/ton, which is not more than one fifth of the heating cost of the traditional technology.
According to the technical scheme, the carbon powder combustion furnace is used for providing high-temperature flue gas for the fluidized bed pyrolysis reactor, the high-temperature flue gas and granular biomass materials are subjected to pyrolysis reaction to generate gasified mixed gas of bio-oil, carbon powder, carbon monoxide, carbon dioxide, hydrogen and the like, the carbon powder is separated through the gas-solid separation device, the recovered carbon powder can be used for combustion in the carbon powder combustion furnace, and the graded condensing device is used for grading and condensing pyrolysis gas to obtain bio-oil. The technical scheme disclosed by the invention can meet (or basically meet) the requirements of a temperature field and a flow field of the fluidized bed pyrolysis reactor by burning the by-product (carbon powder), greatly reduces the production cost of the bio-oil, and implements rapid cooling and fractional condensation according to different condensation points of each component gas, so that multi-grade and multi-purpose bio-oil with relatively enriched components is obtained, the application approach of the bio-oil is effectively widened, and the comprehensive utilization value of the bio-oil is improved.
So far, the embodiments of the present disclosure have been described in detail with reference to the accompanying drawings. It is to be noted that, in the attached drawings or in the description, the implementation modes not shown or described are all the modes known by the ordinary skilled person in the field of technology, and are not described in detail. In addition, the above definitions of the components are not limited to the specific structures, shapes or manners mentioned in the embodiments, and those skilled in the art may easily modify or replace them.
It is also noted that, unless otherwise indicated, the numerical parameters set forth in the specification and attached claims are approximations that can vary depending upon the desired properties sought to be obtained by the present disclosure. In particular, all numbers expressing dimensions, range conditions, and so forth, used in the specification and claims are to be understood as being modified in all instances by the term "about". Generally, the expression is meant to encompass variations of ± 10% in some embodiments, 5% in some embodiments, 1% in some embodiments, 0.5% in some embodiments by the specified amount.
It will be appreciated by a person skilled in the art that various combinations and/or combinations of features described in the various embodiments and/or in the claims of the invention are possible, even if such combinations or combinations are not explicitly described in the invention. In particular, various combinations and/or combinations of the features recited in the various embodiments and/or claims of the present invention may be made without departing from the spirit or teaching of the invention. All such combinations and/or associations fall within the scope of the present invention.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
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