CN113105916A - Biomass baking system and baking method and application thereof - Google Patents
Biomass baking system and baking method and application thereof Download PDFInfo
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- CN113105916A CN113105916A CN202110466690.XA CN202110466690A CN113105916A CN 113105916 A CN113105916 A CN 113105916A CN 202110466690 A CN202110466690 A CN 202110466690A CN 113105916 A CN113105916 A CN 113105916A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention provides a biomass baking system and a baking method and application thereof, belonging to the field of biomass energy. According to the invention, the two processes of baking and ball milling of the biomass are coupled, so that the crushing energy consumption is greatly reduced compared with the direct crushing of the biomass, and the problem of biomass raw material quality in the process of preparing the synthesis gas by adopting a biomass gasification technology is solved; the baking gas is not discharged outside and is used as a carrier gas of the biomass gasification unit to participate in the reaction, so that the energy of the baking gas is utilized, and the pollution to the atmosphere is avoided; the heat exchange is carried out between the baking gas and the flue gas, and then the biomass is directly heated by the obtained high-temperature baking gas, so that the heat exchange efficiency is high, the control is easy, and the method has good practical application value.
Description
Technical Field
The invention belongs to the field of biomass energy, and particularly relates to a biomass baking system and a baking method and application thereof.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
Biomass, which is the energy converted from biomass, is the only renewable energy source that can be converted into liquid fuels. The biomass thermochemical conversion technology has the advantages of high energy conversion rate, easiness in industrialization and the like, and comprises a direct combustion technology, a pyrolysis technology, a gasification technology and a liquefaction technology. The biomass liquefaction technology comprises a direct liquefaction technology and an indirect liquefaction technology, wherein the direct liquefaction technology is also called a pyrolysis liquefaction technology and is used for directly preparing biomass into liquid fuel; the indirect liquefaction technology is that biomass is firstly subjected to directional gasification to obtain synthesis gas, and then hydrocarbon fuel, alcohol fuel and chemicals are synthesized. The directional gasification of biomass for the purpose of producing synthesis gas is essentially different from conventional gasification for the purpose of producing fuel gas, i.e. it is not aimed at the calorific value, but is converted as much as possible to H-rich2CO and CO2The amount of the useless gas and the hydrocarbon in the mixed gas is as small as possible, so that the difficulty of the subsequent reforming conversion is reduced.
The biomass indirect liquefaction technology is one of the technologies with the most development potential for biomass energy utilization, and the gasification process is a key link in the technology. The biomass gasification is mainly divided into two types, namely fixed bed gasification and fluidized bed gasification according to different types of used gasifiers, wherein the fixed bed gasification reactor has a simple structure, is convenient to operate and has a flexible operation mode, but can only be suitable for medium and small-scale production; the fluidized bed gasification furnace has good mixing characteristic and higher gas-solid reaction rate, and is more suitable for industrialization and large-scale production. The raw materials used by the fluidized bed are not limited in type and feeding shape, so that the fluidized bed is more suitable for biomass raw materials with different qualities, but in order to ensure the normal fluidization of the biomass fuel, the fluidized bed has strict requirements on the particle size of the fuel entering the furnace, so that the biomass needs to be subjected to a series of pretreatment such as drying and crushing, and a large amount of energy is consumed in the crushing process.
The problem of quality of biomass raw materials (biomass has the defects of high water content, high oxygen content, difficult storage, difficult crushing and the like) solved by adopting a reasonable pretreatment mode becomes a current research hotspot. The baking technology can greatly improve the physical and chemical properties of the biomass, including obviously improving the milling performance of the biomass, effectively improving the energy density and the bulk density of the biomass, and simultaneously reducing the oxygen content of the biomass, thereby receiving wide attention and attention at home and abroad.
The biomass baking technology is a method for thermally treating biomass under the conditions of low temperature (generally 200-350 ℃), oxygen deficiency and low heating rate, can ensure that cellulose, hemicellulose and lignin in the biomass generate pyrolysis and carbonization to a certain degree, effectively remove moisture and light volatile matters in the biomass, and generate a large amount of solid products (biochar), a certain amount of condensed liquid (bio-oil, water vapor and the like) and non-condensable gas (CO, CO and the like)2And CH4Etc.), so that the raw material quality is improved, and the obtained biochar has the advantages of high heat value, high energy density, strong hydrophobicity, good grindability, no decay, suitability for long-time storage and long-distance transportation and the like, and can be widely applied to the fields of pyrolysis, gasification, power generation, heat supply, flue gas purification, soil improvement and the like.
CN107586567A discloses a biomass pyrolysis gas-carbon clean CO-production process based on continuous dry distillation, gasification reforming and baking coupling treatment, which mainly comprises the procedures of raw material baking pretreatment, continuous dry distillation, gasification reforming and fuel gas recycling heating, wherein the procedures of raw material baking pretreatment, continuous dry distillation, gasification reforming and fuel gas recycling heating improve the production efficiency of a system and realize the efficient and gradient utilization of waste heat through substance and energy coupling conversion and tar reduction, thereby achieving the purpose of clean production, but the process directly adopts flue gas to bake biomass, and then baking gas (containing CO, CO and CO) is generated2、CH4Biological oil, water vapor, etc.) are discharged as exhaust gas along with the flue gas, not only polluting the atmosphere, but also wasting the energy of the baking gas. ZL201820880004.7 discloses an fatlute pyrolysis rotary furnace, and the technical scheme who adopts is provided with the flue gas discharge port for the top of kiln hood cover, and the bottom is provided with the tailings discharge port, and the hot-blast furnace is installed to the bottom of kiln hood, and the hot-blast furnace is linked together through high temperature hot-blast main and kiln hood, and this scheme adopts the hot-blast directness that the hot-blast furnace produced to carry out the pyrolysis to fatlute, and the flue gas of production directly discharges, also has the problem of polluted atmosphere and energy waste.
ZL201410241502.3 discloses a low-quality fuel pyrolysis process, combine dry quenching technology and fluidized bed pyrolysis technology each other, utilize the quenching gas of absorbing the semicoke heat to mix a part of high-temperature flue gas and use as the fluidized medium, and return the fluidized gas after cooling to the dry quenching coke oven and use as the quenching gas, utilize the high-temperature flue gas after the pyrolysis gas burns as the system heat source at the same time, while utilizing the fluidized bed fast pyrolysis technology, the waste heat of the high-temperature semicoke has effectively been absorbed, the thermal efficiency of the system has been improved, and use the fluidized medium of system and the coupling of quenching medium, reduce the quenching cost while guaranteeing the tar yield, realized utilizing fluidized bed technology to produce tar and semicoke simultaneously, this process uses the flue gas in the indirect heating low-quality fuel, the baking gas is not discharged, but the efficiency of indirect heating is lower, difficult to large-scale apparatus control. Furthermore ZL201280029802.4 discloses a method and a system for efficient torrefaction of biomass, said system comprising a first zone for heating optionally pre-dried biomass and an insulated second zone for torrefaction of the heated biomass, the second zone having an inlet connected to an outlet of the first zone and means for withdrawing torrefied biomass disposed at the bottom of the second zone, whereby the biomass can move downwards through the second zone by gravity. CN104039938A discloses a reactor for grinding and torrefying biomass, comprising a chamber delimited by an inner wall interior, a grinding means inside the chamber comprising a rotating central shaft rotatably mounted within the chamber and a grinding element present on the rotating central shaft for grinding biomass, preferably lignocellulosic biomass, present inside the chamber against the inner wall. In all of these patents, biomass is heated by indirect heating with a heating medium (e.g., hot gas), and there are problems that the heating efficiency is low and the control is difficult in large-scale apparatuses.
In conclusion, biomass gasification has the problems of poor biomass raw material quality, high energy consumption for raw material pretreatment, unreasonable heating mode and the like, and the whole links of biomass indirect liquefaction technologies such as drying, baking, pyrolysis, gasification, reforming, steam conversion, purification, fischer-tropsch synthesis, reaction separation and the like of biomass raw materials must be considered from various aspects such as energy utilization, resource utilization, environmental protection and the like, so that a more suitable biomass raw material pretreatment process is selected.
Disclosure of Invention
Aiming at the defects of the prior art, the inventor provides a biomass baking system, a baking method and application thereof through long-term technical and practical exploration.
Specifically, the invention adopts the following technical scheme:
in a first aspect of the invention, there is provided a biomass torrefaction system, comprising:
the ball milling device comprises a rotary furnace, wherein a ball milling medium and a plurality of baffle plates for intercepting the ball milling medium are arranged at one end of the furnace tail of the rotary furnace in a furnace tube of the rotary furnace;
the furnace end of the rotary furnace is provided with a furnace head cover and a spiral feeder, and the furnace tail of the rotary furnace is provided with a furnace tail cover;
the top of the furnace end cover is provided with an exhaust port, and the bottom of the furnace end cover is provided with a dust exhaust port;
the top of the furnace tail cover is provided with an air inlet, and the bottom of the furnace tail cover is provided with a discharge hole;
the pipeline behind the air outlet is divided into two branches, one branch is provided with an exhaust valve, the other branch is communicated with a fan, the pipeline behind the fan is communicated with a heat exchanger, and the pipeline behind the heat exchanger is communicated with an air inlet.
In a second aspect of the invention, a biomass torrefaction method is provided, wherein the torrefaction method is carried out by using the biomass torrefaction system.
Specifically, the baking method comprises the following steps:
the biomass is conveyed to the rotary furnace by the spiral feeder, and is in countercurrent contact with the high-temperature baking gas heated by the heat exchanger in the rotary furnace to generate new baking gas, the baking gas enters the furnace head cover and is then discharged by the exhaust port to be divided into two paths, one path of baking gas is discharged by the exhaust valve, the other path of baking gas is conveyed to the heat exchanger by the fan, and the high-temperature baking gas heated by the heat exchanger enters the furnace tail cover through the air inlet and is in countercurrent contact with the biomass in the rotary furnace;
the dust carried by the baking gas settles in the furnace end cover and is discharged through a dust outlet;
the biomass is baked in a rotary furnace in a rotary mode, becomes charcoal with smaller particles under the action of a ball milling medium, and then enters a furnace tail cover to be discharged through a discharge hole.
In a third aspect of the invention, there is provided the use of the torrefaction system and/or torrefaction process described above in pyrolysis gasification of biomass.
The beneficial technical effects of one or more technical schemes are as follows:
according to the technical scheme, the two processes of baking and ball milling of the biomass are coupled, so that the crushing energy consumption is greatly reduced compared with the direct crushing of the biomass, and the obtained small-particle biochar is easier to control when a fluidized bed is adopted for gasification; the heat exchange is carried out between the baking gas and the flue gas, and then the biomass is directly heated by the obtained high-temperature baking gas, so that the heat exchange efficiency is high and the control is easy; baking gas (containing CO, CO)2、CH4Biological oil, water vapor and the like) are not discharged outside and are used as reaction gases of a subsequent gasification unit and a subsequent reforming unit, so that the energy of the baking gas is utilized, and the pollution to the atmosphere is avoided, thereby having good practical application value.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic view of a biomass torrefaction system according to the present invention.
FIG. 2 is a front view of a rotary kiln of the biomass torrefaction system of the present invention.
In the figure: 101-an exhaust valve; 102-an exhaust port; 103-furnace head cover; 104-a screw feeder; 105-dust exhaust port; 106-pressing ring; 107-filler; 108-a fan; 109-a heat exchanger; 110-a rotary kiln; 111-striker plate; 112. 115-a support bracket; 113-a transmission; 114-ball milling media; 116-an air inlet; 117-furnace tail hood; 118-a discharge hole.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
The terms "a" or "an" herein do not denote a limitation of quantity, but rather denote the presence of at least one of the referenced item. In addition, it should be noted that the terms "upper" and "lower," and the like, as used herein, are used for descriptive purposes only and are not limited to any one position or spatial orientation unless otherwise specified.
As described above, the problems of poor quality of biomass raw materials, high energy consumption for raw material pretreatment, unreasonable heating manner, and the like exist in the current biomass gasification, and a more suitable biomass raw material pretreatment process must be selected in consideration of the whole links of biomass indirect liquefaction technologies such as drying, baking, pyrolysis, gasification, reforming, steam shift, purification, fischer-tropsch synthesis, reaction separation, and the like of the biomass raw materials from various aspects such as energy utilization, resource utilization, environmental protection, and the like.
In view of the above, the invention provides a biomass baking system and a baking method, which couple two processes of baking and ball milling of biomass, so that the crushing energy consumption is greatly reduced compared with the direct crushing of the biomass, and the problem of biomass raw material quality in the process of preparing synthesis gas by using a biomass gasification technology is solved; the baking gas is not discharged outside and is used as a carrier gas of the biomass gasification unit to participate in the reaction, so that the energy of the baking gas is utilized, and the pollution to the atmosphere is avoided; the heat exchange is carried out between the baking gas and the flue gas, and then the biomass is directly heated by the obtained high-temperature baking gas, so that the heat exchange efficiency is high, and the control is easy.
In an exemplary embodiment of the invention, a biomass torrefaction system is provided, the system comprising:
the ball milling device comprises a rotary furnace 110, wherein a ball milling medium 114 and a plurality of material baffle plates 111 for intercepting the ball milling medium 114 are arranged at one end of the furnace tail of the rotary furnace 110 in a furnace tube of the rotary furnace 110;
the furnace head of the rotary furnace 110 is provided with a furnace head cover 103 and a screw feeder 104, and the furnace tail of the rotary furnace 110 is provided with a furnace tail cover 117;
the top of the furnace head cover 103 is provided with an exhaust port 102, and the bottom of the furnace head cover 103 is provided with a dust exhaust port 105;
the top of the furnace tail cover 117 is provided with an air inlet 116, and the bottom of the furnace tail cover 117 is provided with a discharge hole 118;
the pipeline behind the exhaust port 102 is divided into two branches, one branch is provided with an exhaust valve 101, the other branch is communicated with a fan 108, the pipeline behind the fan 108 is communicated with a heat exchanger 109, and the pipeline behind the heat exchanger 109 is communicated with an air inlet 116.
In another embodiment of the present invention, the striker plate 111 is provided with sieve holes, and the maximum diameter of the sieve holes is smaller than the minimum diameter of the ball milling media 114.
The number of the striker plates can be set according to actual conditions, and in a specific embodiment of the invention, the number of the striker plates is 1-6, such as 1, 2, 3, 4, 5 or 6.
In one embodiment of the present invention, the ball milling media have different specifications (diameters), for example, two stainless steel solid balls with diameters of 0.03 m and 0.05 m are provided, so that ball milling is more sufficient.
In another embodiment of the present invention, the furnace head of the rotary furnace 110 passes through the furnace head cover 103 to the inside of the furnace head cover 103, the furnace tail of the rotary furnace 110 passes through the furnace tail cover 117 to the inside of the furnace tail cover 117, and the screw feeder 104 passes through the furnace head cover 103 to the inside of the furnace tube of the rotary furnace 110.
In another embodiment of the present invention, the furnace head cover 103 is a cyclone separator, the furnace head of the rotary furnace 110 is connected to the furnace head cover 103 from the circumferential tangential direction of the top end of the upper portion of the furnace head cover 103, the screw feeder 104 passes through the furnace head cover 103 from the circumferential tangential direction of the top end of the upper portion of the furnace head cover 103 to the interior of the furnace tube of the rotary furnace 110, the circumferential middle of the top of the furnace head cover 103 is provided with the exhaust port 102, and the lower end of the exhaust port 102 extends into the lower portion of the furnace head cover 103.
In another embodiment of the present invention, the outer layers of the rotary kiln 110, the furnace end cover 103 and the furnace tail cover 117 are all provided with insulating bricks.
In another embodiment of the present invention, a pressing ring 106 and a filler 107 are disposed between the furnace head and the furnace head cover 103 of the rotary furnace 110, and a pressing ring 106 and a filler 107 are disposed between the furnace tail of the rotary furnace 110 and the furnace tail cover 117.
In another embodiment of the present invention, the furnace head of the rotary furnace 110 is higher than the furnace tail.
In another embodiment of the present invention, the supporting bracket 112 and the supporting bracket 115 are disposed outside the furnace tube of the rotary kiln 110, and the transmission device 113 is disposed outside the furnace tube of the rotary kiln 110.
In yet another embodiment of the present invention, a biomass torrefaction method is provided, which is performed using the biomass torrefaction system described above.
Specifically, the baking method comprises the following steps:
the biomass is conveyed to a rotary furnace 110 by a screw feeder 104, the biomass is in countercurrent contact with high-temperature baking gas heated by a heat exchanger 109 in the rotary furnace 110 to generate new baking gas, the baking gas enters a furnace end cover 103, then is discharged through an exhaust port 102 and then is divided into two paths, one path of the baking gas is discharged through an exhaust valve 101, the other path of the baking gas is conveyed to the heat exchanger 109 through a fan 108, and the high-temperature baking gas heated by the heat exchanger 109 enters a furnace end cover 117 through an air inlet 116 and is in countercurrent contact with the biomass in the rotary furnace 110;
dust carried by the baking gas settles in the furnace end cover 103 and is discharged through a dust discharge port 105;
the biomass is rotary baked in the rotary kiln 110 and is turned into smaller particles of biochar by the ball milling media 114, and then enters the kiln tail cover 117 and is discharged through the discharge port 118.
In another embodiment of the present invention, the heat exchanger 109 uses high temperature flue gas as a heat source, and the low temperature flue gas coming out of the heat exchanger 109 dries the biomass by direct heating.
In a further embodiment of the invention the torrefaction gas discharged via the exhaust valve 101 is used as reaction gas for subsequent biomass gasification units and reforming units. The biochar discharged through the discharge port 118 is directly used as a raw material of the biomass gasification unit without cooling, or is stored after cooling.
In a further embodiment of the present invention, there is provided the use of the torrefaction system and/or torrefaction process described above in pyrolysis gasification of biomass.
In yet another embodiment of the present invention, the biomass may be agricultural and forestry waste, such as straw (corn stover, wheat straw), edible fungus substrate, bark, peanut shell, bagasse, rice chaff, and the like.
The present invention is further illustrated by reference to specific examples, which are intended to be illustrative only and not limiting. If the specific conditions are not specified in the examples, the conditions are generally in accordance with the conventional conditions or in accordance with the conditions recommended by the sales company; the present invention is not particularly limited, and may be commercially available.
Example 1
As shown in fig. 1 and 2, the biomass torrefaction system comprises a rotary furnace 110, a fan 108 and a heat exchanger 109.
The head of the rotary kiln 110 is provided with a head cover 103 and a screw feeder 104, and the tail of the rotary kiln 110 is provided with a tail cover 117. The outer layers of the rotary furnace 110, the furnace end cover 103 and the furnace tail cover 117 are provided with insulating bricks.
The furnace head of the rotary furnace 110 penetrates through the furnace head cover 103 to the inside of the furnace head cover 103, the furnace tail of the rotary furnace 110 penetrates through the furnace tail cover 117 to the inside of the furnace tail cover 117, and the screw feeder 104 penetrates through the furnace head cover 103 to the inside of the furnace tube of the rotary furnace 110.
A pressing ring 106 and a filler 107 are arranged between a furnace head and a furnace head cover 103 of the rotary furnace 110, and the pressing ring 106 and the filler 107 are arranged between a furnace tail of the rotary furnace 110 and a furnace tail cover 117.
The rotary kiln 110 had a crown higher than a tail with an inclination of 6%.
The top of the furnace head cover 103 is provided with an exhaust port 102, and the bottom of the furnace head cover 103 is provided with a dust exhaust port 105.
An air inlet 116 is arranged at the top of the furnace tail cover 117, and a discharge hole 118 is arranged at the bottom of the furnace tail cover 117.
The pipeline behind the exhaust port 102 is divided into two paths, one path is provided with an exhaust valve 101, the other path is communicated with a fan 108, the pipeline behind the fan 108 is communicated with a heat exchanger 109, and the pipeline behind the heat exchanger 109 is communicated with an air inlet 116.
The outside of the furnace tube of the rotary furnace 110 is provided with a support bracket 112 and a support bracket 115, and the outside of the furnace tube of the rotary furnace 110 is provided with a transmission device 113.
The furnace tube of the rotary furnace 110 is a stainless steel tube, the length of the furnace tube is 5 meters, and the inner diameter is 0.4 meter.
The 5 baffle plates 111 are respectively 0.02 meter, 0.52 meter, 1.02 meter, 1.52 meter and 2.02 meter away from the tail end of the furnace tube of the rotary furnace 110, and divide the furnace tube of the rotary furnace 110 into 5 ball milling areas.
The striker plate 111 is provided with sieve holes.
The ball milling medium 114 adopts stainless steel solid balls with the diameters of 0.03 meter and 0.05 meter respectively, and the number of the two stainless steel solid balls is equal.
The diameter of the sieve holes arranged on the material baffle plate 111 is 0.02 m.
The fan 108 is a CX-1/4 type frequency conversion high temperature resistant fan produced by Jiangsu full wind environmental protection technology limited.
The biomass baking method adopting the baking system comprises the following steps:
corn straws (with the water content of 10 percent by mass) with the length of 0.03 meter are taken as raw materials, the lower calorific value of the raw materials is 14.5MJ/kg, the temperature of the raw materials is 150 ℃, nitrogen is firstly adopted to replace air in the rotary furnace 110 in the baking starting stage, the rotating speed of the rotary furnace 110 is 1.0r/min, then the raw materials are fed into the rotary furnace 110 at the speed of 10kg/h through a screw feeder 104, the raw materials are in countercurrent contact with high-temperature baking gas heated by a heat exchanger 109 in the rotary furnace 110 to generate new baking gas, and the baking gas enters a furnace end cover 103 and is then discharged through an exhaust port 102. The baking gas exhausted through the exhaust port 102 is divided into two paths, one path of the baking gas is exhausted through the exhaust valve 101, the other path of the baking gas is conveyed to the heat exchanger 109 through the fan 108, the high-temperature baking gas obtained by heating through the heat exchanger 109 enters the furnace tail cover 117 through the air inlet 116 and is in countercurrent contact with the biomass in the rotary furnace 110; dust carried by the baking gas settles in the furnace end cover 103 and is discharged through a dust discharge port 105; the biomass is rotary baked in the rotary kiln 110 and is turned into smaller particles of biochar by the ball milling media 114, and then enters the kiln tail cover 117 and is discharged through the discharge port 118.
The heat exchanger 109 takes high-temperature flue gas at 580 ℃ as a heat source, and the low-temperature flue gas coming out of the heat exchanger 109 adopts a drying step of biomass in a direct heating mode.
The torrefaction gas discharged through the exhaust valve 101 is used as a reaction gas for the subsequent biomass gasification unit and the reforming unit. The temperature of the biochar discharged from the discharge port 118 is 305 ℃, and the biochar is directly used as a raw material of the biomass gasification unit without cooling.
The flow rate of the roasting gas passing through the fan 108 and the flow rate of the high-temperature flue gas introduced into the heat exchanger 109 are adjusted so that the temperature of the high-temperature roasting gas heated by the heat exchanger 109 is 530 ℃, and the temperature of the roasting gas discharged through the exhaust port 102 is 175 ℃.
The baking operation was carried out for 10 hours to obtain 38.5kg of biocoke and 0.21kg of dust discharged through the dust discharge port 105. The particle size of the obtained biochar is measured according to the national standard GB-T10322.7-2004 'sieving determination of iron ore particle size distribution', the particle size is less than 2.5 mm and is more than 94.5% (mass percent), and the particle size is less than 4.0 mm and is more than 99.8% (mass percent); the low calorific value of the obtained biochar is measured to be 25.05MJ/kg according to the national standard GB/T213-2008 'method for measuring calorific value of coal'.
In the embodiment, the baking and ball milling processes of the biomass are coupled, so that the biomass is easy to crush; the heat exchange is carried out between the baking gas and the flue gas, and then the biomass is directly heated by the obtained high-temperature baking gas, so that the heat exchange efficiency is high and the control is easy; the baking gas is not discharged outside, so that the energy of the baking gas is utilized, and the pollution to the atmosphere is avoided.
Example 2
The same parts of this embodiment as embodiment 1 will not be described again, but the differences are:
the furnace head cover 103 is a cyclone separator, a furnace head of the rotary furnace 110 is connected with the furnace head cover 103 from the circumferential tangential direction of the top end of the upper part of the furnace head cover 103, the screw feeder 104 penetrates through the furnace head cover 103 from the circumferential tangential direction of the top end of the upper part of the furnace head cover 103 to the interior of a furnace tube of the rotary furnace 110, the exhaust port 102 is arranged in the middle of the circumference of the top of the furnace head cover 103, and the lower end of the exhaust port 102 extends into the lower part of the furnace head.
The baking operation was carried out for 10 hours to obtain 38.7kg of biocoke and 0.44kg of dust discharged through the dust discharge port 105. The particle size of the obtained biochar is measured according to the national standard GB-T10322.7-2004 'sieving determination of iron ore particle size distribution', the particle size is less than 2.5 mm and is more than 94.7% (mass percent), and the particle size is less than 4.0 mm and is more than 99.8% (mass percent); the low calorific value of the obtained biochar is measured to be 25.08MJ/kg by referring to the national standard GB/T213-2008 'method for measuring calorific value of coal'.
The furnace end cover 103 in this embodiment adopts a cyclone separator structure, and can effectively capture dust in the baking gas (the dust is mixed with the raw material and then is continuously baked), thereby improving the operation conditions of pipelines and equipment.
Example 3
The same parts of this embodiment as embodiment 2 will not be described again, but the differences are:
the temperature of the biochar discharged through the discharge hole 118 is 305 ℃, and the biochar is cooled and stored.
The baking was run for 10 hours to obtain 38.6kg of biochar, and 0.45kg of dust discharged through the dust discharge port 105. The particle size of the obtained biochar is measured according to the national standard GB-T10322.7-2004 'sieving determination of iron ore particle size distribution', the particle size is less than 2.5 mm and is more than 94.9% (mass percent), and the particle size is less than 4.0 mm and is more than 99.8% (mass percent); the low calorific value of the obtained biochar is measured to be 25.09MJ/kg by referring to the national standard GB/T213-2008 'method for measuring calorific value of coal'.
The biochar obtained by the embodiment is cooled and stored, so that the quality problem of biomass raw materials is solved, (the biomass has the defects of high water content, high oxygen content, difficulty in storage, difficulty in crushing and the like), and the obtained biochar has the advantages of high heat value, high energy density, strong hydrophobicity, good grindability, no decay, suitability for long-time storage and long-distance transportation and the like.
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (10)
1. A biomass torrefaction system, comprising:
the ball milling device comprises a rotary furnace, wherein a ball milling medium and a plurality of baffle plates for intercepting the ball milling medium are arranged at one end of the furnace tail of the rotary furnace in a furnace tube of the rotary furnace;
the furnace end of the rotary furnace is provided with a furnace head cover and a spiral feeder, and the furnace tail of the rotary furnace is provided with a furnace tail cover;
the top of the furnace end cover is provided with an exhaust port, and the bottom of the furnace end cover is provided with a dust exhaust port;
the top of the furnace tail cover is provided with an air inlet, and the bottom of the furnace tail cover is provided with a discharge hole;
the pipeline behind the air outlet is divided into two branches, one branch is provided with an exhaust valve, the other branch is communicated with a fan, the pipeline behind the fan is communicated with a heat exchanger, and the pipeline behind the heat exchanger is communicated with an air inlet.
2. The biomass torrefaction system according to claim 1, wherein the striker plate is provided with screen holes, the largest diameter of the screen holes being smaller than the smallest diameter of the ball milling media;
preferably, the number of the material baffle plates is 1-6;
the ball milling medium is a stainless steel solid ball; further preferably, the ball milling media have different specifications.
3. The biomass torrefaction system according to claim 1, wherein the burner of the rotary kiln passes through the burner head housing to an interior of the burner head housing, the tail of the rotary kiln passes through the tail housing to an interior of the tail housing, and the screw feeder passes through the burner head housing to an interior of the furnace tube of the rotary kiln;
preferably, the furnace end cover is a cyclone separator, the furnace end of the rotary furnace is connected with the furnace end cover from the circumferential tangent direction of the top end of the upper part of the furnace end cover, the spiral feeder penetrates through the furnace end cover from the circumferential tangent direction of the top end of the upper part of the furnace end cover to the interior of the furnace tube of the rotary furnace, the exhaust port is arranged in the middle of the circumference of the top of the furnace end cover, and the lower end of the exhaust port extends into the lower part of the furnace end cover.
4. The biomass torrefaction system according to claim 1, wherein the outer layers of the rotary kiln, the kiln head hood and the kiln tail hood are provided with insulating bricks.
5. The biomass torrefaction system according to claim 1, wherein a pressing ring and a filler are disposed between a furnace head and a furnace head cover of the rotary furnace, and a pressing ring and a filler are disposed between a furnace tail and a furnace tail cover of the rotary furnace;
preferably, the furnace head of the rotary furnace 110 is higher than the furnace tail.
6. The biomass torrefaction system according to claim 1, wherein the supporting brackets are disposed on the exterior of the furnace tube of the rotary kiln, and the transmission device is disposed on the exterior of the furnace tube of the rotary kiln.
7. A biomass torrefaction process, wherein the torrefaction process is performed using the biomass torrefaction system according to any one of claims 1 to 6.
8. The biomass torrefaction process of claim 7, wherein the torrefaction process comprises:
the biomass is conveyed to the rotary furnace by the spiral feeder, and is in countercurrent contact with the high-temperature baking gas heated by the heat exchanger in the rotary furnace to generate new baking gas, the baking gas enters the furnace head cover and is then discharged by the exhaust port to be divided into two paths, one path of baking gas is discharged by the exhaust valve, the other path of baking gas is conveyed to the heat exchanger by the fan, and the high-temperature baking gas heated by the heat exchanger enters the furnace tail cover through the air inlet and is in countercurrent contact with the biomass in the rotary furnace;
the dust carried by the baking gas settles in the furnace end cover and is discharged through a dust outlet;
the biomass is baked in a rotary furnace in a rotary manner, becomes smaller-grained biochar under the action of a ball milling medium, and then enters a furnace tail cover to be discharged through a discharge hole;
preferably, the heat exchanger takes high-temperature flue gas as a heat source, and the low-temperature flue gas coming out of the heat exchanger dries the biomass in a direct heating mode;
preferably, the torrefaction gas discharged through the exhaust valve is used as a reaction gas for the subsequent biomass gasification unit and the reforming unit; the biochar discharged from the discharge port is directly used as a raw material of the biomass gasification unit without cooling, or is cooled and stored.
9. Use of the torrefaction system according to any one of claims 1 to 6 and/or the torrefaction method according to any one of claims 7 to 8 for pyrolysis gasification of biomass.
10. The use of claim 9, wherein the biomass comprises agricultural and forestry waste;
preferably, the agricultural and forestry waste includes, but is not limited to, straw, edible fungus substrate, bark, peanut shell, bagasse and rice chaff.
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