CN116376578B - Continuous carbonization method and equipment for biomass waste by utilizing aerodynamic method - Google Patents
Continuous carbonization method and equipment for biomass waste by utilizing aerodynamic method Download PDFInfo
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a biomass waste continuous carbonization method and equipment by utilizing a gas dynamic method, wherein the method comprises pretreatment, process control and feeding, carbonization, carbon-gas separation, energy self-supply and gas self-circulation; the method for determining the technological parameters comprises the steps of obtaining physical characteristics of the straw, obtaining performance parameters of carbonization equipment, establishing a thermodynamic equation, solving the technological parameters of a production process, and checking the effectiveness of the technological parameters; the equipment comprises a venturi tube, a blower, a feed controller, a hopper, a multi-layer tower carbonization furnace, a cooling discharge mechanism, a gas distributor, a burner and a gas mixer. The method and the equipment thereof have the advantages of continuous carbonization, real-time treatment, high carbonization efficiency, large yield, compact equipment structure, portability and the like.
Description
Technical Field
The invention relates to the field of biomass waste, in particular to a biomass waste continuous carbonization method and equipment by utilizing a gas dynamic method.
Background
A large amount of straw can be produced in the agricultural production process. The traditional agricultural straw disposal mode mainly adopts field incineration, and is converted into grass-mesh ash for returning to the field, but the field incineration mode can cause environmental pollution and resource waste. The existing straw crushing and direct returning technology is beneficial to increasing soil organic matters and improving soil physical and biological properties. However, the contradiction between soil microorganisms (namely, microorganisms converted from straw) and crop seedlings competing for nutrients can be increased, and even phenomena such as yellow seedlings, dead seedlings, yield reduction and the like occur. In particular to insect eggs, bacteria and other diseases and insect pests in the straw, which are left in the soil after returning to the field, and the diseases and insect pests directly occur or occur in winter.
The straw carbonization returning technology can effectively solve the problems of germs, ova, insect pests and the like existing in the direct returning of the straw. Straw carbonization and returning are technical routes which take biomass straw carbon as a main development direction, can realize multiple targets of straw comprehensive utilization, soil structure improvement, increase of agricultural carbon sink, reduction of greenhouse gas emission and the like.
The agricultural straw carbonization technology is an important guarantee for realizing straw carbonization and returning to the field. However, conventional biomass carbonization equipment, such as a soil kiln, a fixed bed carbonization furnace, a rotary kiln carbonization furnace and the like, are limited due to the excessively high transportation and storage costs of straws. Moreover, the problems of long carbonization period, high operation cost, low production efficiency and the like of the existing carbonization equipment are difficult to be practically applied to the field of pyrolysis carbonization of agricultural straws.
The straw carbonization technology is popularized and developed in rural areas, and the following key technical problems need to be solved. First, the carbonization of agricultural straw needs to have continuous real-time property, the pyrolysis carbonization process of the straw can be continuously produced and can be completed in a short time, and only then the on-line treatment requirement of the agricultural straw can be met. Secondly, the carbonization of agricultural straws needs to have high efficiency, and the carbonization capacity of ten tons and tens of tons per day is required to be achieved, so that the treatment requirement of a large amount of farmland straws can be met only. Thirdly, the agricultural straw carbonization needs to have low cost, and the movable carbonization equipment is developed to realize field carbonization and returning to the field, so that the collection and transportation cost of the straw is effectively reduced. Therefore, the development of a novel continuous, efficient and low-cost agricultural straw carbonization technology and equipment thereof is a key for realizing straw carbonization and returning to the field.
Disclosure of Invention
The invention provides a biomass waste continuous carbonization method and equipment by utilizing a gas dynamic method, in particular to straws, which solve the problems that the carbonization period of the straws is long and the real-time on-site straw disposal cannot be satisfied in the prior art.
The process and the equipment thereof provided by the invention not only can be used for agricultural straws (wheat straws, rice straws, hemp stalks, tobacco straws, corn stalks, cotton stalks and the like), but also can be used for the treatment and carbonization of other biomass wastes (such as bamboo chips, bamboo shoot skins, branches and leaves, paper, broken cloth, plastic sheets, organic films and the like) with similar physical properties to the straws.
In order to facilitate feeding and carbonization, the agricultural straw is firstly crushed into short diameters with the length of 50mm or less in the process. And then introducing a gas dynamic theory and a method, and feeding by using high-speed high-temperature gas (gas phase) carrying straw short diameter (solid phase). The short diameter of the straw of the independent solid phase forms a certain dynamic pressure difference before and after the short diameter in a high-speed high-temperature gas phase environment. The dynamic pressure difference enables the short diameter of the straw to be always in a suspension state, and forms a speed difference and a dynamic pressure difference of relative motion with the gas phase. Under the action of the speed difference and the dynamic pressure difference, high-speed gas molecules impact the short-diameter surface of the straw violently, and intense gas-solid phase suspension heat exchange is generated between the gas phase and the solid phase.
The short diameter of the straw in a suspension state changes at high speed and randomly, so that the uniformity of gas-solid phase heat exchange is effectively ensured. In order to further improve the heat exchange efficiency between the gas phase and the solid phase, the invention designs a closed arc-shaped pyrolysis pipeline to form a pyrolysis carbonization space. Therefore, under the action of centrifugal force, the short diameter of the straw is concentrated on the outer side of the arc pyrolysis pipeline and is contacted and rubbed with the outer wall of the high-temperature arc pipeline to a certain extent. Direct contact conduction heat exchange is generated between the solid phases to provide energy for short-diameter pyrolysis of the straw. Therefore, the invention provides a continuous, efficient and real-time straw continuous carbonization technology.
The technical scheme of the invention is realized as follows:
a method for continuously carbonizing biomass waste by utilizing a gas dynamic method, comprising:
(1) Pretreatment of biomass waste: screening soil carried in biomass waste, and crushing the screened biomass waste to short diameter or particles;
(2) Process control and feeding:
putting the short diameter or the particles into a pyrolysis carbonization space; and then performing process control:
the process control is to control the rotating speed of a blower to ensure that the high-temperature gas speed in the pyrolysis carbonization space is constant as the gas process speedVThe method comprises the steps of carrying out a first treatment on the surface of the Controlling the rotation speed of the feeder to ensure that the raw materials in the hopper are fed in the short diameter or the particleMFeeding; controlling the mixing proportion of the hot gas and the high-temperature gas to ensure that the temperature of the mixed high-temperature gas reaches the gas process temperatureT；
(3) Carbonizing:
after feeding, the short diameter or the particle diameter is in a severe suspension and friction alternate motion state, and the short diameter or the particle is suspended and advanced in the pyrolysis carbonization space and is thrown to the outer wall of the pyrolysis carbonization space under the action of centrifugal force, contacted with the outer wall of the pyrolysis carbonization space and rubbed; during the movement, the minor diameter or particles are carbonized;
the carbonization is carried out with heat exchange, and under the action of the heat exchange, the surfaces and the interiors of the short diameter or particles form a high-speed heating rate and reach the carbonization temperature rapidlytRealizing the high-speed carbonization of biomass waste; the temperature of the high temperature gas is also determined by the gas process temperatureTRapidly decrease to carbonization temperaturet；
And (3) carbon gas separation: separating out biomass waste carbon powder suspended in high-temperature gas, discharging the biomass waste carbon powder through a carbon outlet and cooling the biomass waste carbon powder; recycling high-temperature gas without carbon powder;
the high-temperature gas is divided into two parts by a distributor: part of the fuel is used as gaseous fuel to be sent into a gas burner for combustion, and chemical energy of high-temperature gas is released; the other part is sent into the mixer as high-temperature gas, and the physical latent heat of the high-temperature gas is provided;
(5) Energy is self-supplied: the high-temperature gas is combusted in the gas burner, and chemical energy is released to generate hot gas with the temperature of more than 700 ℃; the hot gas is divided into two parts: a part of the water is sent into a drying system to provide a heat source for short-diameter dehydration treatment; another part is sent into the mixer for energy self-supply, in the mixer, the temperature of the high-temperature gas is controlled by carbonization temperaturetRe-rising to the gas process temperatureT；
(6) Gas self-circulation:
the self-circulation is two, and the first is to reintroduce the high-temperature gas in the step (5) into the carbonization system to realize the gas self-circulation; the second is that the temperature of the high-temperature gas is at the carbonization temperaturetAnd gas process temperatureTPeriodically reciprocating between them.
In some embodiments, the biomass waste is crushed to a short diameter or particle of 50mm or less.
In some embodiments, the short diameter or particle is dried to dehydrate such that the water content of the short diameter or particle is 20% or less. If the biomass waste has been exposed to the sun, the water content is below 20%, this step may be omitted. The dried biomass waste is temporarily stored in a feed hopper (or raw material bin) in a short diameter.
In some embodiments, the biomass waste is straw, bamboo chips, bamboo shoot skin, branches and leaves, paper, rag, plastic sheet, or organic film.
In some embodiments, the total flow and cross-sectional flow of the high temperature gas is constant during the two cycles.
The carbonization has three heat exchange processes at the same time: the first is gas-solid phase suspension heat exchange between high-temperature gas and short diameter straw; the second is the gas-solid phase radiation heat exchange between the high temperature gas and the pipe wall; and thirdly, solid-solid phase conduction heat exchange by contact friction between the outer wall of the pipeline and the short diameter of the straw. Under the combined action of the three heat exchanges, the surface and the inside of the short diameter of the straw form a high-speed heating rate and quickly reach the carbonization temperaturetRealize high-speed carbonization of the straw. The temperature of the high temperature gas is also determined by the gas process temperatureTRapidly decrease to carbonization temperaturet。
The method for determining the technological parameters of continuous carbonization of biomass waste by utilizing the aerodynamic method is characterized by comprising the following steps:
(1) Obtaining physical characteristics of straw:
sampling the dry short diameter to be treated, and obtaining the following 4 characteristic parameters: free fall speedvSpecific heatC b Specific heat of combustion flue gasC a Water contentw；
(2) Obtaining performance parameters of carbonization equipment:
the following 3 equipment performance parameters are obtained through field measurement and physical test of carbonization equipment: equivalent diameter of pyrolysis pipeDCoefficient of resistance of smoke in pipelineλ a Along-path resistance coefficient of straw in pipelineλ b ；
(3) Establishing a 'dynamic equation': according to the theory of gas dynamics, a description of the state of short-path motion is established, which satisfies the requirement of high-temperature gas (gas process speedV) Constraint conditions capable of enabling the short diameter to be always in a suspension state; wherein the equation has the form:
wherein ,λ a the resistance coefficient is the on-way resistance coefficient of the high-temperature gas, and is dimensionless;λ b the resistance coefficient is the along-path resistance coefficient of the short diameter, and is dimensionless;Tthe temperature is the gas process temperature, and the unit is the temperature;Dis the equivalent diameter of the pyrolysis pipeline area, and the unit is m; g is gravitational acceleration, unit N/kg;vthe free falling speed in the high-temperature gas environment with a short diameter is in m/s;Vis the gas process speed, unit m/s;Mbiomass waste feed amount per kg/s;
(4) Establishing a thermodynamic equation: according to thermodynamic principles, a description of the heat exchange between the hot gas and the short path is established, the equation satisfying the requirements of the hot gas (gas process speedVProcess temperature of gasT) The feeding amount can be adjustedMThe short diameter of (2) is heated from normal temperature to carbonization temperaturetIs a constraint on (2); the program has the following form:
wherein ,C a specific heat of high-temperature gas (equivalent specific heat of straw combustion flue gas can be used), per Kcal/kg ℃;C p the specific heat of water vapor can be obtained by looking up a table, and the unit Kcal/kg ℃;C b the specific heat of the straw is per Kcal/kg ℃;tthe carbonization temperature is given in units of ℃;wthe water content of the straw is dimensionless;
(5) Solving the technological parameters of the production process: firstly, according to the amount of biomass waste to be treatedPresetting biomass waste feeding amountMThen vector is usedV，T) For solving the strain quantity, the dynamic equation in the step (3) and the thermodynamic equation in the step (4) are combined to form an equation set for solving;
(6) Checking the validity of the technological parameters: process parameters (charge amount) obtained by simultaneous solvingMProcess speed of gasVAnd gas process temperatureT) Checking; for the technological parameters meeting the failure conditions, the preset straw feeding amount is reducedMAnd returning to the step (5), the first failure condition is set up as follows: gas process speedVThe product of the cross-sectional area of the pyrolysis pipeline and the cross-sectional area of the pyrolysis pipeline is larger than the maximum flow of the blower; the second failure condition established is: gas process temperatureTIs larger than the heat-resistant temperature of the material used by the arc pyrolysis pipeline. For example, the heat resistant temperature of carbon steel is 600 ℃, the heat resistant temperature of 304 stainless steel is 800 ℃, and the heat resistant temperature of 310S stainless steel is 1100 ℃.
A biomass waste continuous carbonization apparatus using a aerodynamic method, comprising:
the device comprises a venturi tube, a blower, a feeding controller, a hopper, a multi-layer tower carbonization furnace, a cooling discharging mechanism, a gas distributor, a burner and a gas mixer;
the venturi tube, the blower, the multi-layer tower carbonization furnace, the gas distributor and the gas mixer are sequentially connected in series and form a high-temperature gas circulation channel; the hopper is arranged above the feeding controller, and the feeding controller is arranged above the feeding port of the venturi tube, so that the raw materials in the hopper can be adjusted to enter the venturi tube through the feeding controller;
the multi-layer tower carbonization furnace consists of a plurality of layers of spiral pipelines and tower cores 5-9 which are nested from outside to inside; the spiral pipeline is formed by sequentially spiraling an arc pyrolysis pipeline in the same direction in a cylindrical tubular shape, and the inner wall of the outer spiral pipeline is the outer wall of the inner spiral pipeline; the cross section of the arc pyrolysis pipeline is rectangular; the multi-layer tower carbonization furnace is provided with the heat preservation layer only on the outer side of the spiral pipeline at the outermost layer, and conduction heat exchange is carried out between the layers in the multi-layer tower carbonization furnace without heat preservation;
the spiral pipeline at the outermost layer of the multi-layer tower carbonization furnace spirals from bottom to top or from top to bottom in the same direction; the secondary outer layer spiral pipeline spirals from top to bottom or from bottom to top in the same direction, and so on; the spiral pipelines of all layers from outside to inside are sequentially connected in series;
the inner wall of the outer layer pyrolysis pipeline is provided with heat conducting fins which are in the same direction with the air flow direction in the multi-layer tower carbonization furnace so as to improve the gas-solid phase heat exchange capacity of the air to the heat conducting surface of the inner wall; the outer wall of the inner layer pyrolysis pipeline is also provided with heat conducting fins in the same direction as the airflow direction, so that the solid-solid phase heat conduction efficiency of the contact friction between the heat conducting surface of the outer wall and the short diameter of the straw is improved;
the tower core is the innermost spiral pipeline of the multi-layer tower carbonization furnace; the arc-shaped pyrolysis pipeline of the tower core spirals from top to bottom in the same direction, and the lower wall of the arc-shaped pyrolysis pipeline shortens outwards until disappearing in the process of spiraling from top to bottom; the bottom of the tower core is provided with a conical receiving hopper; the bottom of the receiving hopper is provided with a carbon outlet and is connected with a cooling discharging mechanism, so that the straw carbon powder is discharged after being cooled; the inner wall of the arc pyrolysis pipeline of the tower core forms a central pipe, and the high-temperature gas is led out of the multi-layer tower carbonization furnace through the central pipe.
In some embodiments, the temperature of the hot gas generated after combustion is above 700 ℃.
In some embodiments, the gas distributor is a three-way structure, one inlet, a first outlet, and a second outlet; the inlet is connected with the multi-layer tower carbonization furnace, and high-temperature gas discharged by the multi-layer tower carbonization furnace is introduced; the second outlet is connected with the burner; the first outlet is connected with the gas mixer; the gas distributor is internally provided with a regulating valve or a regulating mechanism, and the proportion of the gas distributed by the first outlet and the second outlet can be regulated.
In some embodiments, the burner is a combustible gas combustion device that generates hot gas after combustion; the burner is provided with two high temperature outlets: a first high temperature outlet and a second high temperature outlet; the first high-temperature outlet is connected with the gas mixer and is used for synthesizing high-temperature gas; and the second high-temperature outlet is connected with an air inlet of a spray tower of the drying system or the purifying system.
In some embodiments, the gas mixer is a channel-shaped high-temperature mixing chamber, one end of the high-temperature mixing chamber is a first inlet, and the other end of the high-temperature mixing chamber is an outlet; a second inlet is arranged in the middle part or near the inlet side of the high-temperature mixing chamber; the first inlet is connected with a first high-temperature outlet of the combustor, and hot gas is introduced; the second inlet is connected with the first outlet of the gas distributor, and high-temperature gas is introduced; the outlet is connected back to the venturi tube and the blower; the gas mixer is provided with a valve or an adjusting mechanism, and the mixing proportion of the hot gas and the high-temperature gas can be adjusted according to the temperature of the gas at the outlet.
Compared with the prior art, the invention has the following beneficial effects:
(1) Carbonization is continuous and real-time treatment. The high-speed heating rate of more than 10 ℃/s is formed on the surface and inside of the short diameter of the straw, so that the straw can reach pyrolysis temperature and complete carbonization within tens of seconds, and the requirement of continuous real-time carbonization of the agricultural straw is met.
(2) High charring efficiency and high output. The detention time of the straw in the device is short, and the straw disposal has the characteristic of fast-in and fast-out. Therefore, the process can reach the straw disposal capacity of tens of tons/day.
(3) The device has compact structure and is movable. The device adopts an integrated structural design, has small volume, can be installed on a moving platform of a vehicle, and can move at any time according to straw disposal requirements. The device is agricultural mechanical equipment, can realize the on-site treatment of agricultural and forestry waste, converts the transportation of the straw into the movement of the device, and remarkably reduces the operation cost.
Drawings
In order to more clearly illustrate the embodiments of the invention or the technical solutions in the prior art, the drawings which are used in the description of the embodiments or the prior art will be briefly described, it being obvious that the drawings in the description below are only some embodiments of the invention, and that other drawings can be obtained from them without inventive faculty for a person skilled in the art.
FIG. 1 is a process flow diagram of the present invention.
Fig. 2 the invention provides a schematic structural view of the device.
Wherein: (1) venturi, (1-1) venturi inlet, (1-2) venturi throat, (1-3) venturi outlet, (1-4) venturi feed inlet 1-4, (2) blower, (3) feed controller, (4) hopper, (5) multi-layer tower carbonization furnace, (5-3) multi-layer tower carbonization furnace inlet, (5-4) insulation, (5-14) multi-layer tower carbonization furnace outlet, (6) cooling discharge mechanism, (7) gas distributor, (7-1) gas distributor inlet 7-1, (7-2) gas distributor first outlet, (7-3) gas distributor second outlet, (7-4) gas distributor valve plate, (8) burner, (8-1) combustion chamber, (8-2) refractory furnace, (8-3) insulation, (8-4) gas combustion lance, (8-5) air blower, (8-6) first high temperature outlet, (8-7) second high temperature outlet, (9) mixing chamber, (9-1) mixing chamber first inlet, (9-2) mixing chamber second inlet; (9-3) a mixing chamber outlet; (9-4) high Wen Zha plate valve, (9-5) butterfly valve.
Fig. 3 is a schematic structural view of the outermost spiral pipe.
Wherein, (5-1) the outermost spiral pipeline, (5-2) the arc pyrolysis pipeline, (5-3) the inlet 5-3 of the multi-layer tower carbonization furnace; (5-4) an insulating layer.
Fig. 4 is a cross-sectional view of the outermost and layer 2 helical piping structures.
Wherein, (5-1) an outermost spiral pipeline, (5-2) an arc pyrolysis pipeline and (5-3) a multi-layer tower carbonization furnace inlet; (5-4) heat insulation layer, (5-5) layer 2 spiral pipeline.
Fig. 5 is a schematic view of the location of the straw minor diameter in the pyrolysis tube.
Wherein, (5-2) arc pyrolysis pipeline, (5-7) heat conduction fin, (5-8) straw short diameter.
FIG. 6 is a cross-sectional view of a tower core structure.
Wherein, (5-3) the inlet of the multi-layer tower carbonization furnace, (5-9) the tower core, (5-10) the lower wall of the pipeline, (5-11) the receiving hopper, (5-12) the carbon outlet, (5-13) the central pipe and (5-14) the outlet of the multi-layer tower carbonization furnace.
FIG. 7A is a cross-sectional view of a refractory block.
Wherein, (8-1) combustion chamber, (8-2) refractory furnace body, (8-3) interlayer, and (9) mixing chamber.
Fig. 7B is an oblique view of the mixing chamber structure.
Wherein, (8-2) refractory furnace, (8-3) interlayer, (9-1) mixing chamber first inlet, (9-2) mixing chamber second inlet, (9-3) mixing chamber outlet.
Description of the embodiments
The following description of the technical solutions in the embodiments of the present invention will be clear and complete, and it is obvious that the described embodiments are only some embodiments of the present invention, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention.
The invention provides a continuous carbonization method of straw by utilizing a gas dynamic method and equipment thereof, which can use agricultural straw as a raw material to prepare straw carbon; but the method and the equipment are not limited to straw, and can be used for carbonizing other types of biomass waste. The equipment can independently operate, and can also be matched with equipment such as an external drying system, a storage bin, a conveyor belt, a spiral feeder, tail gas environmental protection disposal and the like.
In this embodiment, taking corn stalk treatment as an example, a specific embodiment of a stalk continuous carbonization method using aerodynamic method according to the present invention is described in further detail with reference to fig. 1:
a continuous carbonization process for straw by utilizing a gas dynamic method comprises the following steps:
(1) Pretreatment of corn stalks: screening out soil carried in the corn straws by using a rolling screen, and crushing the corn straws to a short diameter with the granularity of less than 50mm by using a straw crusher;
(2) Drying and dehydrating: because the corn stalks are exposed to the sun after autumn harvest, the water content is 10% -18%, and the corn stalks do not need to be dried again. Directly storing the dry corn stalk short diameter in a raw material bin.
(3) Parameter acquisition: taking a corn straw short-diameter sample and performing physical test to obtain relevant physical characteristic parameters of the straw short-diameter: free fall speedvSpecific heat of straw flue gasC a Specific heat of strawC b Moisture content of straww The method comprises the steps of carrying out a first treatment on the surface of the And then measuring and looking up a table of the carbonization equipment to obtain the performance parameters of the equipment: equivalent diameter D of pyrolysis pipeline area and on-way resistance coefficient of straw in pipelineλ b Along-path resistance coefficient of high-temperature flue gasλ a The method comprises the steps of carrying out a first treatment on the surface of the Average specific heat of water vaporC p Obtained by checking handbook, the carbonization temperature of the corn strawtObtained by a horse boiling furnace experiment at 350 ℃.
(4) And (3) determining process parameters: by using the parameters and according to the theory of gas dynamics, the gas process speed of the high-speed high-temperature gas is improvedVThe requirement that the short diameter of the straw is always in a suspension state is needed, and a corresponding 'dynamic equation' is established. And then according to the thermodynamic heat exchange principle, a corresponding thermodynamic equation is established for the heat exchange of the gas phase and the solid phase to meet the requirement of thermodynamic equilibrium. In the embodiment, the corn stalk treatment requirement is about 1 ton/hr, so that the stalk feeding amount can be obtainedMAt 0.3kg/s, the two equation sets are combined to solve the gas process speedVAt a gas process temperature of 7.2m/sTIs 460 ℃.
(5) Process control and feeding: a closed arc-shaped pyrolysis pipeline is adopted as a pyrolysis carbonization space, and the short diameter of the straw is put into the arc-shaped pyrolysis pipeline. 3 technological parameters in the production process are controlled while feeding; the specific process control method in this embodiment is: and detecting the actual flow rate of the high-temperature gas in the arc pyrolysis pipeline in the multi-layer tower carbonization furnace by using a high Wen Fengsu instrument. The frequency converter is used for controlling the rotating speed of the blower motor, so that the flow speed of the actual high-temperature gas is 7.2m/s. The star-shaped blanking device is arranged at the bottom of the raw material bin, and the rotation speed of the motor of the star-shaped blanking device is used for adjusting the feeding quantity of the corn straw so as to ensure that the corn straw is stabilized at 0.3kg/s. Finally, detecting the actual temperature of the high-temperature gas at the outlet of the gas mixer by using a thermocouple; and the mixing proportion of the hot gas and the high-temperature gas is adjusted by utilizing an adjusting mechanism in the gas mixer: the hot gas duty cycle is increased if the actual temperature of the hot gas is lower than 460 ℃, and the hot gas duty cycle is increased if the actual temperature of the hot gas is higher than 460 ℃.
(6) High-speed carbonization of corn stalks: the short diameter of the corn straw is controlled to be in a suspension state in the arc pyrolysis pipeline. In the embodiment, the average heating rate of the surface and the inside of the corn straw is about 10 ℃/s, and the corn straw is heated to the pyrolysis temperature of 350 ℃ from normal temperature in about 40 seconds and continuous real-time carbonization is completed. The temperature of the high temperature gas is also reduced from the gas process temperature of 460 ℃ to the carbonization temperature of 350 ℃.
(7) And (3) carbon gas separation: and a gravity dust removal separator or a multi-layer tower type carbonization furnace core is selected as a separation mechanism to separate the corn stalk carbon powder from high-temperature gas at 350 ℃. The carbon powder is cooled, discharged and packaged by a water-cooling screw arranged at the bottom of the separating mechanism. The high-temperature gas without carbon powder is led out from the separating mechanism to the distributor. The distributor is internally provided with an adjusting valve. The high-temperature gas is divided into two parts by the regulating valve of the distributor: part of the fuel is used as gaseous fuel to be sent into a gas burner for combustion, and chemical energy of high-temperature gas is released; the other part is sent as a high temperature gas to the mixer to provide the physical latent heat of the high temperature gas.
(8) Energy is self-supplied: the high-temperature gas entering the gas burner is combusted, chemical energy of the high-temperature gas is released, and hot gas with the temperature of more than 700 ℃ is generated. In the embodiment, about 3/4 of hot air can be sent into the drying system to provide a heat source for the short-diameter dehydration treatment of the straw. For the case that the moisture content of the corn stalks is about 15% and drying is not needed in the embodiment, the hot gas can be directly introduced into the purification spray tower for discharge. About 1/4 of the hot gas is fed into the mixer and the mixing ratio of the high-temperature gas and the hot gas is adjusted by using the adjusting valve. The temperature of the high temperature gas was allowed to rise again from 350 to 460 ℃. Therefore, in the embodiment, the energy required by pyrolysis and carbonization of the corn straw is derived from the corn straw, and no additional energy is needed.
(9) Gas self-circulation: in the process of the invention, the self-circulation of the high temperature gas comprises two circulation: first, the circulation of the hot gas itself. After the high-temperature gas is led out of the mixer, the high-temperature gas returns to the mixer again through the Venturi tube, the blower, the arc pyrolysis pipeline, the carbon separation mechanism and the distributor, and is repeatedly utilized and recycled; second, the temperature of the high-temperature gas is controlled by the arc pyrolysis tubeTCooling totThen in the mixer is formed bytRe-heating toTThe method comprises the steps of carrying out a first treatment on the surface of the In the process of technological circulation, the high-temperature gas is subjected to physical temperature rise, temperature reduction and re-temperature rise, …, and the temperature of the gas is at the carbonization temperaturetAnd gas process temperatureTAnd periodically reciprocally circulated. And the total flow and the section flow of the high-temperature gas are constant in the two circulation processes.
In the embodiment, the high-temperature gas is heated from 350 ℃ to 460 ℃ in the mixer, then enters the venturi tube again, and is blown into the arc pyrolysis pipeline by the blower; after heat exchange between the high-temperature gas and the corn stalks in a suspended state, the temperature of the high-temperature gas is reduced to 350 ℃. Then the high-temperature gas re-enters the mixer after passing through the gas-carbon separation mechanism and the distributor, and the high-temperature gas is repeatedly utilized and reciprocally circulated; during this cycle, the hot gas undergoes physical warming, cooling, reheating, …, thus reciprocating. Thus, in this embodiment, the high temperature gas is always in a gas self-circulation state, the total flow rate and flow velocity of the high temperature gas are constant, and the high temperature gas is periodically and reciprocally circulated at a temperature of 350 ℃ to 460 ℃ along with the process.
Examples
A method for determining technological parameters of continuous carbonization of straw by utilizing a gas dynamic method comprises the following steps:
and obtaining the physical characteristics of the corn straw. The physical test is carried out on the corn stalk short diameter with dry sampling noise, and the free falling speed of the corn stalk short diameter of 50mm is measured by utilizing upward air flow measurementv4.7m/s; by specific heat measurementMeasuring specific heat of corn stalk by constant instrumentC b 0.45Kcal/kg ℃; high-temperature flue gas specific heat for measuring straw combustion by using specific heat determinatorC a 0.255Kcal/kg ℃; corn stalk water content determination by using a horse boiling furnace and national standard methodw15%.
(2) And obtaining the performance parameters of the carbonization equipment. Actually measuring an arc-shaped pyrolysis pipeline in carbonization equipment to obtain an equivalent diameter D of the pyrolysis pipeline area of 0.25m; measuring the in-path resistance coefficient of high-temperature flue gas generated by straw combustion by using in-path resistance coefficient measuring experiment instrumentλ a 0.0455; obtaining the on-way resistance coefficient of the straw short diameter in the pipeline by using an on-way resistance coefficient measurement experiment instrumentλ b 0.004; table lookup to obtain average specific heat of water vaporC p 0.51Kcal/kg ℃; the carbonization temperature of the corn straw is obtained through a horse boiling furnace experimentt350 ℃;
(3) A "kinetic equation" is established. According to the theory of gas dynamics, the gas process speed of the high-speed high-temperature gas is used in the inventionVThe condition that the short diameter of the straw is always in a suspension state is needed, and a corresponding 'dynamic equation' can be established:
wherein g is the gravitational acceleration, here 9.8N/kg.
(4) A "thermodynamic equation" is established. According to thermodynamic heat exchange principle, high-speed high-temperature gas (gas process speedVProcess temperature of gasT) The short diameter of the straw is required to be heated from normal temperature to carbonization temperaturetCan establish a corresponding "thermodynamic equation":
in the two equations set forth above,Vis the gas process speed and the gas process temperatureTStraw feeding amountMFor the work of the production process to be determinedProcess parameters.
(5) Solving the technological parameters of the production process. In the embodiment, the corn stalk treatment requirement is about 1 ton/hr, so that the stalk feeding amount can be obtainedM0.3kg/s; will beMSubstituting the two equations to solve the gas process speedVAt a gas process temperature of 7.2m/sTIs 460 ℃.
(6) Checking the validity of the technological parameters. First, in this embodiment, the maximum flow rate of the blower is 2000m 3/hr (i.e., 0.55m 3/s); the cross section area of the pyrolysis pipeline is 0.04m 2, so that the gas process speed is highVThe product of the cross section of the pipeline and the cross section of the pipeline is 0.288m & lt 3 & gt/s, which is smaller than the maximum flow of the blower; second, in this embodiment, the arc-shaped pyrolysis tube is made of carbon steel, and the heat-resistant temperature of the carbon steel is 600 ℃ which is higher than the required gas process temperature of 460 ℃. Therefore, the process parameters found in this example: straw feeding amountMIs 0.3kg/s and gas process speedVAt a gas process temperature of 7.2m/sTIs effective at 460 ℃.
Example 3
The invention also provides a straw continuous carbonization device utilizing the aerodynamic method. The following describes in further detail a specific embodiment of a continuous carbonization device for straw using aerodynamic method according to the present invention with reference to fig. 2:
a continuous carbonization device for straw using aerodynamic method, comprising: a venturi tube 1, a blower 2, a feeding controller 3, a hopper 4, a multi-layer tower carbonization furnace 5, a cooling discharging mechanism 6, a gas distributor 7, a burner 8 and a gas mixer 9.
The length of the venturi tube 1 is 1.5m, the diameter of the inlet 1-1 is 0.25mm, the diameter of the middle throat opening 1-2 is 0.15, the diameter of the outlet 1-3 is 0.25mm, the feeding opening 1-4 is arranged above the throat opening, and the opening size of the feeding opening 1-4 is 200mm multiplied by 200mm.
The blower 2 is a centrifugal blower with the full pressure of 500Pa, the flow rate of 2000m < 3 >/h and the highest temperature of 600 ℃.
The feeding controller 3 selects a star-shaped blanking device with an opening of 200mm multiplied by 200mm and a blanking speed of 10m & lt 3 & gt/h.
The hopper 4 is an inverted cone-shaped raw hopper with the length of 1m, the width of 1m and the depth of 0.8m, and the opening size of the bottom of the raw hopper is 200mm multiplied by 200mm.
The multi-layer tower carbonization furnace 5 adopts a 4-layer tower carbonization furnace structure, namely, the multi-layer tower carbonization furnace is formed by mutually nesting 4 layers of spiral pipelines from outside to inside, the outer diameter is 1.8m, and the height is 2.0m; the structural schematic of the outermost layer (layer 1) spiral pipe 5-1 is shown in fig. 3; the outermost spiral pipeline 5-1 is formed by arc pyrolysis pipeline 5-2 in a cylindrical tubular shape in turn and spirals from bottom to top in a anticlockwise direction; an inlet 5-3 is arranged below the outermost spiral pipeline 5-1; the cross section of the arc pyrolysis pipeline 5-2 is a square with the size of 200mm multiplied by 200 mm; the outside of the outermost spiral pipeline is also provided with a heat preservation layer 5-4. The multilayer tower carbonization furnace 5 has the advantages that: first, the length of the arc pyrolysis tube is greatly increased in a limited space; the design is beneficial to the miniaturization and the mobility of the equipment; secondly, an insulating layer is arranged only on the outer side of the spiral pipeline at the outermost layer (namely the outer wall of the pyrolysis pipeline at the layer), the upper, lower and inner sides of the pyrolysis pipeline at the layer do not need to be insulated, and all the spiral pipelines at each layer in the layer do not need to be insulated; this design is advantageous in reducing heat radiation and heat loss from the device.
The layer 2 spiral pipeline 5-5 is spirally wound from top to bottom in a anticlockwise direction by using the arc pyrolysis pipeline 5-2; the inner wall 5-6 of the outermost layer spiral pipeline 5-1 is the outer wall of the layer 2 spiral pipeline 5-5; a cross-sectional view of the structure of the outermost spiral pipe 5-1 and the 2 nd spiral pipe 5-5 is shown in FIG. 4.
The temperature of the spiral pipeline 5-1 at the outermost layer of the multi-layer tower carbonization furnace 5 is highest; the heat energy conducts heat to the inside of the layer 2 spiral pipeline 5-5 by taking the inner wall 5-6 of the outermost layer spiral pipeline 5-1 as a heat conducting surface. Due to the centrifugal force, the straw is always concentrated on the outer wall of the arc-shaped pyrolysis tube 5-2 and rubbed with it. The high-temperature gas and the straw are separated to a certain extent, and the distribution is very unfavorable for gas-solid phase heat exchange, so that the carbonization efficiency of the invention is affected. Therefore, in the equipment provided by the invention, the outer wall of the inner pyrolysis pipeline and the inner wall of the outer pyrolysis pipeline are respectively welded with the heat conducting fins 5-7 which are in the same direction with the air flow direction. The heat conduction fins 5-7 of the outer layer can absorb the heat energy of high-temperature gas which is not contacted with the short diameter of the straw at the outer layer, and the heat conduction fins 5-7 of the inner layer are directly contacted with the short diameter of the corn straw, so that the solid-solid phase conduction heat exchange is directly carried out, and the carbonization efficiency of the equipment is improved very effectively. The installation of the heat conducting fin and the relation between the heat conducting fin and the short diameter 5-8 of the straw are shown in figure 5.
The innermost layer (layer 4) spiral pipeline of the multi-layer tower carbonization furnace 5 is a tower core 5-9, and the structural section view of the tower core 5-9 is shown in figure 6; the arc pyrolysis tube 5-2 of the tower core 5-9 spirals from top to bottom in a anticlockwise direction, and the lower wall 5-10 of the tube shortens outwards until disappearing in the spiral process; the bottom of the tower core 5-9 is provided with a conical receiving hopper 5-11; the bottom of the receiving hopper 5-11 is provided with a carbon outlet 5-12; the inner wall of the tower core 5-9 forms a central pipe 5-13; after the lower wall 5-10 of the arc pyrolysis pipeline is shortened, high-temperature gas without carbon powder can be discharged from the pyrolysis pipeline 5-2 layer by layer from top to bottom and is converged in the tower core central pipe 5-13; the high-temperature gas is led out of the multi-layer tower carbonization furnace 5 through the outlets 5-14. After the high-temperature gas is discharged from the pyrolysis pipeline 5-2 layer by layer, the gas flow rate in the pyrolysis pipeline 5-2 of the tower core can be obviously reduced, so that the short diameter of the large-particle corn straw can be remained in the tower core for a longer time, and the carbonization stability and consistency of the short diameter of the large-particle corn straw are ensured.
The functions and design advantages of the tower cores 5-9 are two: the first is that the arc pyrolysis pipeline 5-2 in the interior can still provide pyrolysis carbonization space and heat exchange for the short diameter of the straw; and the second is that after the lower wall 5-10 of the arc pyrolysis pipeline is shortened, the high-temperature gas without carbon powder can be discharged from the pyrolysis pipeline 5-2 layer by layer from top to bottom and is converged in the tower core central pipe 5-13. The working principle of the tower core as a separating mechanism is different from that of the traditional cyclone dust collector, after the high-temperature gas is partially discharged from the pyrolysis pipeline 5-2, the airflow velocity of the pyrolysis pipeline 5-2 in the tower core can be reduced, so that the long-time retention of the large-particle straw short diameter in the tower core is realized, and the small-particle carbon powder is hardly influenced. Therefore, the short diameter of the large-particle straw can be effectively carbonized in the equipment. The design is an important supplement to the high-speed carbonization process used in the invention, and ensures the consistency of the carbonization of the short diameters of the straws with different granularity. Therefore, the design of the multi-layer tower type carbonization furnace 5 realizes the effect of a pyrolysis and separation integrated structure and the effect of carbonization consistency with different granularity.
The cooling discharging mechanism 6 adopts an internal and external double-water-cooling spiral, the spiral length is 3.5 meters, the pitch is 300 mm, the inner diameter is 273mm, and the outer diameter is 450mm.
The gas distributor 7 is designed into a three-way structure, one inlet 7-1, a first outlet 7-2 and a second outlet 7-3, and a valve plate 7-4 is arranged in the gas distributor; the valve plate rotation angle is driven by an electromagnetic controller to adjust the ratio of the air output of the first outlet 7-2 and the second outlet 7-3.
The burner 8 adopts a gas combustion device, and consists of a combustion chamber 8-1, a mixing chamber 9 and a refractory furnace body 8-2; the refractory furnace body 8-2 is a cylindrical furnace body with the inner length of 2.5m and the inner diameter of 1.5m built by high-temperature refractory bricks; the interlayer 8-3 is arranged in the fireproof furnace body 8-2 to divide the space in the fireproof furnace body 8-2 into the combustion chamber 8-1 and the mixing chamber 9. A schematic cross-sectional view of the refractory block is shown in FIG. 7A, and a schematic perspective view of the mixing chamber structure is shown in FIG. 7B.
The combustion chamber 8-1 comprises a gas combustion spray gun 8-4, an air distribution blower 8-5, a first high temperature outlet 8-6 and a second high temperature outlet 8-7. Wherein, the gas combustion spray gun 8-4 adopts 30 ten thousand large card power; the air distribution blower 8-5 is a normal temperature centrifugal blower with the full pressure of 500Pa and the flow rate of 1000m < 3 >/h; the first high-temperature outlet 8-6 is arranged on the interlayer 8-3, the opening size is 200mm multiplied by 200mm, and the combustion chamber 8-1 is communicated with the mixing chamber 9; the second high temperature outlet 8-7 is arranged above the refractory furnace body 8-3, and the flue opening is 200mm multiplied by 200mm.
The mixing chamber 9 is a channel-shaped high-temperature mixing chamber; one end of the channel is provided with a first inlet 9-1 which is communicated with a first high-temperature outlet 8-6 of the burner 8; a second inlet 9-2 is arranged at the middle reverse position of the channel; the other end of the channel is provided with an outlet 9-3; a high Wen Zha plate valve 9-4 is arranged at the first inlet 9-1; a butterfly valve 9-5 is arranged at the second inlet 9-2; a thermocouple is arranged at the outlet 9-3 of the mixing chamber 9 to detect the temperature of the mixed high-temperature gas; if the temperature after mixing is lower, increasing the opening of the high-temperature gate valve 9-4 and simultaneously reducing the opening of the butterfly valve 9-5; vice versa, until the temperature of the hot gas reaches the gas process temperature T.
Negative pressure feeding was used for the physical properties of the corn stover used in this example. The inlet of the blower 2 is connected with the outlet 1-3 of the venturi tube 2, the outlet of the blower 2 is connected with the inlet 5-3 of the multi-layer tower carbonization furnace 5, the outlet 5-14 of the multi-layer tower carbonization furnace 5 is connected with the inlet 7-1 of the gas distributor 7, the first outlet 7-2 of the gas distributor 7 is connected with the second inlet 9-5 of the mixing chamber 9 through the butterfly valve 9-5, and finally the outlet 9-3 of the mixing chamber 9 is connected back to the inlet 1-1 of the venturi tube 1, so that a closed-loop gas circulation channel is formed.
The hopper 4 is arranged above the feed controller 3, and the feed controller 3 is arranged above the feed inlet 1-4 of the venturi tube 1, so that the raw materials in the hopper 4 can be fed through the feed controller 3 to the venturi tube 1.
The cooling discharging mechanism 6 is arranged below the carbon outlet 5-12 of the multi-layer tower carbonization furnace 5, cools the high-temperature corn straw carbon powder, and discharges and packages the cooled straw carbon powder.
The second outlet 7-3 of the gas distributor 7 is connected with the gas combustion spray gun 8-4 of the burner 8; the second high temperature outlet 8-7 of the burner 8 is connected to the inlet of the purification system spray tower 10.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features can be replaced equivalently; such modifications and substitutions do not depart from the spirit of the invention.
Claims (4)
1. A method for continuously carbonizing biomass waste by using a gas dynamic method, which is characterized by comprising the following steps:
(1) Pretreatment of biomass waste: screening soil carried in biomass waste, crushing the screened biomass waste to a short diameter, wherein the biomass waste is straw;
(2) Process control and feeding:
putting the short diameter into a pyrolysis carbonization space; and then performing process control:
the process control is to control the rotating speed of a blower to ensure that the high-temperature gas speed in the pyrolysis carbonization space is constant as the gas process speedVThe method comprises the steps of carrying out a first treatment on the surface of the Controlling the rotation speed of the feeder to enable the raw materials in the hopper to be fed in the short diameterMFeeding; controlling the mixing proportion of the hot gas and the high-temperature gas without carbon powder to ensure that the temperature of the mixed high-temperature gas reaches the gas process temperatureT；
(3) Carbonizing:
after feeding, the short diameter is in a severe suspension and friction alternate motion state, and the short diameter is suspended and advanced in the pyrolysis carbonization space and is thrown to the outer wall of the pyrolysis carbonization space under the action of centrifugal force, contacted with the outer wall of the pyrolysis carbonization space and rubbed; during the movement, the short diameter is carbonized;
the carbonization is carried out with heat exchange, and the surface and the inside of the short diameter are heated up at high speed under the action of the heat exchange and reach the carbonization temperature rapidlytRealizing the high-speed carbonization of biomass waste; the temperature of the high temperature gas is also determined by the gas process temperatureTRapidly decrease to carbonization temperaturet；
(4) And (3) carbon gas separation: separating out biomass waste carbon powder suspended in high-temperature gas, discharging the biomass waste carbon powder through a carbon outlet and cooling the biomass waste carbon powder; recycling high-temperature gas without carbon powder;
the high-temperature gas without carbon powder is divided into two parts by a distributor: part of the fuel is used as gaseous fuel to be sent into a gas burner for combustion, and chemical energy of high-temperature gas is released; the other part is sent into the mixer to provide the physical latent heat of the high-temperature gas;
(5) Energy is self-supplied: the high-temperature gas without carbon powder is combusted in the gas burner, and chemical energy is released to generate hot gas with the temperature of more than 700 ℃; the hot gas is divided into two parts: a part of the water is sent into a drying system to provide a heat source for short-diameter dehydration treatment; another part is sent outInto the mixer for energy self-supply, in which the temperature of the high-temperature gas is controlled by carbonization temperaturetRe-rising to the gas process temperatureT；
(6) Gas self-circulation:
the self-circulation is two, and the first is to reintroduce the high-temperature gas in the mixer in the step (5) into the carbonization system to realize the self-circulation of the gas; the second is that the temperature of the high-temperature gas is at the carbonization temperaturetAnd gas process temperatureTPeriodically reciprocating between the two;
the method for determining the technological parameters of continuous carbonization of biomass waste comprises the following steps:
(1) Obtaining physical characteristics of straw:
sampling the dry short diameter to be treated, and obtaining the following 4 characteristic parameters: free fall speedvSpecific heatC b Specific heat of combustion flue gasC a Water contentw；
(2) Obtaining performance parameters of carbonization equipment:
the following 3 equipment performance parameters are obtained through field measurement and physical test of carbonization equipment: equivalent diameter of pyrolysis pipeDCoefficient of resistance of smoke in pipelineλ a Along-path resistance coefficient of straw in pipelineλ b ；
(3) Establishing a 'dynamic equation': according to the aerodynamic theory, establishing a description of the motion state of the short diameter, wherein the equation meets the constraint condition that the short diameter is always in a suspension state; the equation has the form:
；
wherein g is gravitational acceleration;
(4) Establishing a thermodynamic equation: according to thermodynamic principles, a description of the heat exchange between the hot gas and the short path is established, the equation satisfying the quantity to be fedMThe short diameter of (2) is heated from normal temperature to carbonization temperaturetIs a constraint on (2); the squareThe program has the following form:
；
wherein ,C p specific heat for water vapor;
(5) Solving the technological parameters of the production process: firstly, presetting the biomass waste feeding amount according to the biomass waste amount to be treatedMThen vector is usedV，T) For solving the strain quantity, the dynamic equation in the step (3) and the thermodynamic equation in the step (4) are combined to form an equation set for solving;
(6) Checking the validity of the technological parameters: biomass waste feeding amount obtained by simultaneous solvingMProcess speed of gasVAnd gas process temperatureTChecking; for the technological parameters meeting the failure conditions, the preset biomass waste feeding amount is reducedMAnd returning to the step (5), the first failure condition is set up as follows: gas process speedVThe product of the cross-sectional area of the pyrolysis pipeline and the cross-sectional area of the pyrolysis pipeline is larger than the maximum flow of the blower; the second failure condition established is: gas process temperatureTIs larger than the heat-resistant temperature of the material used by the arc pyrolysis pipeline.
2. The continuous carbonization method of biomass waste by aerodynamic method according to claim 1, wherein the biomass waste is crushed to a short diameter of 50mm or less.
3. The continuous carbonization method of biomass waste by aerodynamic method according to claim 1, wherein the short diameter is dried and dehydrated so that the water content of the short diameter is 20% or less.
4. The continuous carbonization method of biomass waste by using aerodynamic method according to claim 1, wherein the total flow and the cross-sectional flow of the high-temperature gas entering the pyrolysis carbonization space are constant during the gas self-circulation process.
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