CN117210247A - Method for preparing synthesis gas by gasifying biomass entrained flow - Google Patents
Method for preparing synthesis gas by gasifying biomass entrained flow Download PDFInfo
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- CN117210247A CN117210247A CN202311481946.XA CN202311481946A CN117210247A CN 117210247 A CN117210247 A CN 117210247A CN 202311481946 A CN202311481946 A CN 202311481946A CN 117210247 A CN117210247 A CN 117210247A
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Abstract
The invention belongs to the technical field of biomass recycling, and particularly relates to a method for preparing synthesis gas by biomass entrained-flow bed gasification. According to the method for preparing the synthesis gas by gasifying the biomass entrained-flow bed, coal dust or coal water slurry is not adopted, specifically, biomass dry powder is conveyed into an entrained-flow bed gasifier in a spiral feeding conveying mode, and gasification reaction is carried out under the condition that oxygen and water vapor exist, so that the synthesis gas is obtained; and dense-phase pneumatic conveying is accompanied in the spiral feeding conveying process. According to the invention, biomass dry powder is taken as a raw material, and is conveyed to the entrained-flow gasifier by adopting a conveying mode of combining spiral feeding conveying with dense-phase pneumatic conveying, so that the phenomena of strong water absorption and agglomeration of the dry powder prepared from biomass can be effectively avoided, the biomass conveying amount of unit carrier gas is improved, the difficult problem of low energy density of biomass is overcome, the utilization rate of biomass is improved, and the high-efficiency conversion of biomass energy is realized.
Description
Technical Field
The invention belongs to the technical field of biomass recycling, and particularly relates to a method for preparing synthesis gas by biomass entrained-flow bed gasification.
Background
Biomass refers to various organisms produced by photosynthesis using the atmosphere, water, land, etc., and has the characteristics of reproducibility, low pollution, wide distribution, and abundant resources. Biomass energy is energy stored in the form of chemical energy in biomass, i.e. energy with biomass as a carrier. The biomass energy is mainly utilized by three ways of direct combustion, thermochemical conversion and biochemical conversion. The traditional mode of biomass direct combustion is a firewood stove, the thermal efficiency is lower, generally 20-30%, and a large amount of carbon dioxide is generated in the combustion process, so that the environment-friendly requirement is not met. The biochemical conversion of biomass mainly comprises biomass-biogas conversion and biomass-ethanol conversion, long-time fermentation is needed, and the biomass treatment efficiency per unit time is low.
The biomass thermochemical conversion technology is a technology for gasifying, carbonizing, pyrolyzing and catalytically liquefying biomass under certain conditions to produce gaseous fuel, liquid fuel and chemical substances, and most of the existing biomass thermochemical conversion technologies are biomass fixed bed gasification, hydrothermal carbonization, pyrolysis and the like, so that the biomass energy can be efficiently utilized, but most of the processes are intermittent feeding or intermittent production, and continuous production is difficult to realize. The above problems can be solved by the current technology of co-processing waste materials by gasifying coal water slurry, which is generally to add biomass into organic slurry (slurry obtained by replacing part of coal in coal water slurry with hazardous waste or other substances) for gasification reaction. However, when the technology is adopted to carry out gasification reaction on biomass, the addition amount is difficult to break through 10 percent, and the utilization rate of the biomass is low.
Disclosure of Invention
In view of the above, the invention aims to provide a method for preparing synthesis gas by gasifying a biomass entrained flow bed, which uses biomass dry powder as a raw material, improves the utilization rate of biomass by a conveying mode of combining spiral feeding conveying with dense-phase pneumatic conveying, and realizes efficient conversion of biomass energy.
In order to achieve the above object, the present invention provides the following technical solutions:
a method for preparing synthesis gas by biomass entrained-flow bed gasification does not adopt coal dust or coal water slurry, and comprises the following steps:
conveying biomass dry powder into an entrained flow gasifier in a spiral feeding and conveying mode, and carrying out gasification reaction under the condition of oxygen and water vapor to obtain the synthesis gas;
and dense-phase pneumatic conveying is accompanied in the spiral feeding conveying process.
Preferably, the particle size of the biomass dry powder is less than or equal to 0.5mm, and the water content is less than or equal to 10wt%.
Preferably, the carrier gas used for dense phase pneumatic conveying is carbon dioxide or nitrogen.
Preferably, the pressure of the carrier gas in the conveying process is 2-6 MPa, and the ratio of the mass of the biomass dry powder to the volume of the carrier gas is more than or equal to 100kg/m 3 。
Preferably, the mass ratio of the volume of the oxygen to the biomass dry powder is 400-700 m 3 :1t; the pressure of the water vapor is 2-6 MPa.
Preferably, the gasification reaction is carried out at a temperature of 1000-1600 ℃, a pressure of 0.5-5 MPa and a time of 4-12 s.
Preferably, the gasification reaction also yields a component in the molten state, and the gasification reaction further comprises: and (3) quenching the gas phase component and the molten phase component obtained by the gasification reaction by adopting a water cooling mode to obtain synthesis gas and solid slag respectively.
Preferably, the flow of the chilling water used for chilling water quenching is 6-10 times of the conveying flow of the biomass dry powder.
Preferably, the quenching water is further quenched to obtain chilled ash water, and the quenching ash water further comprises: and (3) cooling and depressurizing the chilled ash water in sequence, and filtering the chilled ash water, and then recycling the chilled ash water for quenching.
Preferably, the quenching water further comprises: and (3) performing gas phase washing and dust removal on gas phase components obtained after quenching water by gas-liquid separation to obtain synthesis gas.
The beneficial effects are that: the invention provides a method for preparing synthesis gas by biomass entrained-flow bed gasification, which does not adopt coal dust or coal water slurry and comprises the following steps: conveying biomass dry powder into an entrained flow gasifier in a spiral feeding and conveying mode, and carrying out gasification reaction under the condition of oxygen and water vapor to obtain the synthesis gas; and dense-phase pneumatic conveying is accompanied in the spiral feeding conveying process. According to the invention, biomass dry powder is taken as a raw material, and is conveyed to the entrained-flow gasifier by adopting a conveying mode of combining spiral feeding conveying with dense-phase pneumatic conveying, so that the phenomena of strong water absorption and agglomeration of the dry powder prepared from biomass can be effectively avoided, the biomass conveying amount of unit carrier gas is improved, the difficult problem of low energy density of biomass is overcome, the utilization rate of biomass is improved, and the high-efficiency conversion of biomass energy is realized.
Drawings
FIG. 1 is a flow chart of a method for preparing synthesis gas by gasification of biomass entrained flow in an embodiment of the invention.
Detailed Description
The invention provides a method for preparing synthesis gas by biomass entrained-flow bed gasification, which does not adopt coal dust or coal water slurry and comprises the following steps:
conveying biomass dry powder into an entrained flow gasifier in a spiral feeding and conveying mode, and carrying out gasification reaction under the condition of oxygen and water vapor to obtain the synthesis gas;
and dense-phase pneumatic conveying is accompanied in the spiral feeding conveying process.
In the present invention, unless otherwise specified, all materials used are commercially available products well known to those skilled in the art or are prepared by methods well known to those skilled in the art.
According to the invention, coal dust or coal water slurry is not adopted, only biomass dry powder is used as a raw material, and a specific material conveying mode is adopted to prepare the synthesis gas, so that the utilization rate of the biomass dry powder is effectively improved. In the invention, the particle size of the biomass dry powder is preferably less than or equal to 0.5mm, more preferably 0.01-0.5 mm, and even more preferably 0.1-0.3 mm; the water content is preferably not more than 10wt%, more preferably 3 to 10wt%, and still more preferably 5 to 8wt%.
In the invention, the biomass dry powder is preferably prepared from biomass raw materials, wherein the biomass raw materials preferably comprise one or more of agriculture and forestry waste, livestock waste and waste generated by taking plants as raw materials through chemical processes; the biomass feedstock preferably comprises solid biomass and/or liquid biomass; the solid biomass preferably includes at least one of oily fruit-based biomass, solid rod-shaped biomass, and powdery biomass; specifically, the oily fruit biomass can be peanut, sesame, rapeseed or thunberg fritillary bulb, and the oily fruit biomass is high-calorific-value biomass with a calorific value higher than 15000J/g; the solid rod-shaped biomass can be straw biomass; the powdery biomass can be specifically Chinese medicine fermentation residues. The biomass dry powder is preferably prepared by selecting a proper method according to the size and the water content of the biomass raw material, and the method is specifically described below.
In the present invention, when the water content of the biomass raw material does not satisfy the above-mentioned requirement, the present invention preferably dehydrates the biomass raw material, and the manner of dehydration preferably includes drying, torrefaction or pyrolysis; the temperature of the drying is preferably 80-180 ℃, more preferably 105-150 ℃; the drying time is preferably 0.5-24 hours, more preferably 1-8 hours; the baking temperature is preferably 180-300 ℃, more preferably 200-250 ℃; the baking time is preferably 0.5-24 hours, more preferably 3-8 hours; the pyrolysis temperature is preferably 350-800 ℃, more preferably 400-600 ℃; the pyrolysis time is preferably 0.5-12 hours, more preferably 3-8 hours. In the present invention, when the biomass raw material is a solid rod-shaped biomass (such as straw-type biomass) or a powdery biomass, the dehydration is preferably oven drying; when the biomass feedstock is an oily fruit-based biomass (such as peanut, sesame, rapeseed or fritillary bulb), the dewatering is preferably torrefaction; when the biomass feedstock is solid rod-shaped biomass and the main component is lignin, the dewatering is preferably pyrolysis under anaerobic conditions to carbonize the biomass feedstock.
In the invention, when the water content of the biomass raw material is more than or equal to 45wt%, the biomass raw material is preferably subjected to solid-liquid separation so as to remove part of free water, and then the obtained solid material is dehydrated according to the technical scheme, so that the energy consumption is reduced. In the present invention, the solid-liquid separation is preferably performed by centrifugation; the rotation speed of the centrifugation is preferably 2000-12000 r/min, more preferably 5000-8000 r/min; the centrifugation time is preferably 0.5 to 2 hours, more preferably 1 to 1.5 hours. The present invention preferably reduces the water content of the resulting solid material to below 45wt% by said centrifugation.
In the present invention, when the size of the biomass raw material does not satisfy the above-mentioned requirements, the present invention preferably sequentially subjects the biomass raw material to milling and sieving, and the milling is preferably performed in a mill to ensure that the sieved biomass dry powder satisfying the particle size requirements is obtained. The biomass dry powder is preferably prepared by pyrolyzing, grinding and sieving the oversize product obtained by sieving again. The invention changes the fiber structure of the oversize material by pyrolysis, which is favorable for obtaining biomass dry powder meeting the requirements of granularity and water content by grinding and sieving.
In the invention, when the biomass raw material has larger size, such as solid rod-shaped biomass, the solid rod-shaped biomass is preferably crushed until the size of the obtained crushed material is less than or equal to 1cm, and then the operation such as dehydration, grinding and the like is carried out according to the requirement; the crushing is preferably shear crushing.
After biomass dry powder is obtained, the invention adds the biomass dry powder in a spiral wayAnd conveying the material to an entrained-flow gasifier in a material conveying mode, and carrying out gasification reaction under the condition of the existence of oxygen and water vapor to obtain the synthesis gas. In the invention, dense phase pneumatic conveying is accompanied in the spiral feeding conveying process. In the invention, the carrier gas used for dense-phase pneumatic conveying is preferably carbon dioxide or nitrogen; the pressure of the carrier gas in the conveying process is preferably 2-6 MPa, and can be specifically 2MPa, 2.5MPa, 3MPa, 3.5MPa, 4MPa, 4.5MPa, 5MPa, 5.5MPa or 6MPa; the ratio of the mass of the biomass dry powder to the volume of the carrier gas is preferably more than or equal to 100kg/m 3 More preferably 100 to 200kg/m 3 Specifically, it may be 100kg/m 3 、110kg/m 3 、120kg/m 3 、130kg/m 3 、140kg/m 3 、150kg/m 3 、160kg/m 3 、170kg/m 3 、180kg/m 3 、190kg/m 3 Or 200kg/m 3 。
In the present invention, the specific operation steps of delivering the biomass dry powder to the entrained-flow gasifier preferably include: the biomass dry powder is placed in a biomass bin, the biomass bin is stamped by adopting low-pressure gas, so that the biomass dry powder is conveyed into a pressurizing bin, carrier gas is introduced into the pressurizing bin for pressurizing after the pressurizing bin is closed by a stop valve, a discharging valve of the pressurizing bin is opened after pressurizing is completed, so that the biomass dry powder is conveyed into a feeding hopper, a bottom discharging hole of the feeding hopper is communicated with a screw feeder, a material output pipe of the screw feeder is communicated with a feeding hole of an entrained-flow gasification furnace, and carrier gas is supplemented to a material output pipe of the screw feeder in the process of conveying the biomass dry powder from the feeding hopper to the screw feeder, so that the biomass dry powder is conveyed into the entrained-flow gasification furnace. In the present invention, the pressure of the low-pressure carrier gas is preferably 0.1 to 3mpa, more preferably 0.4 to 2.5mpa, further preferably 0.8 to 2mpa, still further preferably 1 to 1.5mpa; the pressure in the pressurized storage bin after the pressurization is completed is preferably 1-20 MPa, more preferably 1.2-10 MPa, further preferably 1.3-5 MPa, further preferably 1.4-4 MPa, further preferably 1.5-3 MPa, and further preferably 1.6-2 MPa; the pressure of the additional carrier gas is preferably 0.1 to 20MPa, more preferably 0.5 to 10MPa, further preferably 1 to 5MPa, further preferably 1.5 to 4MPa, further preferably 2 to 3.5MPa, and further preferably 2.5 to 3MPa.
The invention adopts a mode of combining spiral feeding and conveying with dense-phase pneumatic conveying, can effectively avoid the phenomena of strong water absorption and agglomeration of dry powder prepared from biomass, improves the biomass conveying capacity of unit carrier gas, and makes up the difficult problem of lower energy density of biomass, thereby improving the utilization rate of biomass and realizing the efficient conversion of biomass energy; specifically, the energy density and the mass density of the biomass dry powder are lower than those of coal dust, and the biomass combustion heating value per unit mass is insufficient, so that in the gasification process in the entrained flow gasifier, if the temperature in the entrained flow gasifier needs to be kept stable, the biomass material adding amount needs to be increased.
The gasification reaction is carried out in the presence of oxygen and water vapor. In the present invention, the ratio of the volume of oxygen to the mass of biomass dry powder (i.e., O 2 Preferably 400 to 700 m/C oxygen ratio) 3 :1t, may be specifically 400m 3 ：1t、450m 3 ：1t、500m 3 ：1t、550m 3 ：1t、600m 3 ：1t、650m 3 :1t or 700m 3 :1t; the conveying flow of the biomass dry powder is not particularly limited, and the biomass dry powder can be determined according to the treatment capacity in the actual production process. The invention preferably preheats the oxygen and then conveys the oxygen to the entrained flow gasifier through an oxygen delivery pipeline; the preheating temperature is preferably not less than 150 ℃, more preferably 160-180 ℃, and even more preferably 170-180 ℃. In the invention, the pressure of the water vapor is preferably 2-6 MPa, and can be specifically 2.1MPa, 2.5MPa, 3MPa, 3.5MPa, 4MPa, 4.5MPa, 5MPa, 5.5MPa or 6MPa; the invention preferably leads the superheated steam into the oxygen delivery pipelineAnd the superheated steam is conveyed into the entrained-flow gasifier through the oxygen conveying pipeline, the gaseous steam is ensured to be not lower than the dew point temperature in the conveying process, and the steam in the entrained-flow gasifier meets the pressure requirement. In the embodiment of the invention, the entrained-flow gasifier is provided with a gasification nozzle, the material output pipe and the oxygen transmission pipeline of the screw feeder are respectively communicated with the gasification nozzle, and in the actual production process, the biomass dry powder, oxygen and superheated steam are conveyed into the entrained-flow gasifier through the gasification nozzle at the same time for gasification reaction.
In the invention, the temperature of the gasification reaction is preferably 1000-1600 ℃, specifically 1050 ℃, 1100 ℃, 1150 ℃, 1200 ℃, 1250 ℃, 1300 ℃, 1350 ℃, 1400 ℃, 1450 ℃, 1500 ℃, 1550 ℃ or 1600 ℃; the pressure of the gasification reaction is preferably 0.5-5 MPa, and can be specifically 0.5MPa, 1MPa, 1.5MPa, 2MPa, 2.5MPa, 3MPa, 3.5MPa, 4MPa, 4.5MPa or 5MPa; the gasification reaction time is preferably 4-12 s, and may specifically be 4s, 5s, 6s, 7s, 8s, 9s, 10s, 11s or 12s.
In the present invention, the gasification reaction also yields a component in a molten state, and the gasification reaction preferably further comprises: and (3) quenching the gas phase component and the molten phase component obtained by the gasification reaction by adopting a water cooling mode to obtain synthesis gas and solid slag respectively. In the invention, the flow rate of the chilling water used for chilling water quenching is preferably 6-10 times, more preferably 7-8 times, the conveying flow rate of the biomass dry powder. The invention preferably carries out chilling water quenching on the gas phase component and the molten phase component obtained after gasification reaction; the invention adopts a water cooling mode to quench water, which is beneficial to ensuring the stable performance of the synthesis gas preparation process, and the quenching water quenching can lead the gas phase components generated by gasification reaction to be rapidly cooled, thereby avoiding generating dioxin and obtaining cleaner synthesis gas; the molten state component is mainly inorganic matters, the molten state component is fully contacted with chilled water, the glassy water quenching slag formed by the conversion of insoluble matters is the solid slag, and heavy metals can be fixed in the solid slag; the solid slag is preferably used for preparing building materials. The invention preferably discharges the solid slag into a slag collecting tank, and discharges the solid slag into a slag dragging tank after water supplementing by punching.
In the present invention, the quenching water preferably further comprises: and (3) performing gas phase washing and dust removal on gas phase components obtained after quenching water by gas-liquid separation to obtain synthesis gas. In the present invention, the gas-liquid separation is preferably performed in a cooling gas-water separator; the gas phase scrubbing and dust removal is preferably carried out in a scrubbing tower, and the scrubbing liquid used for the gas phase scrubbing and dust removal is preferably water. In the present invention, H is formed during the gasification reaction 2 CO and CO 2 And (3) waiting for gas. In the invention, the effective gas components in the synthesis gas preferably comprise hydrogen and carbon monoxide, and the total volume fraction of the effective gas components in the synthesis gas is preferably more than or equal to 70%, more preferably more than or equal to 75%, and even more preferably 80-83%; the volume fraction of hydrogen in the synthesis gas is preferably 30-42%, more preferably 35-42%, and even more preferably 41-42%. In an embodiment of the invention, the synthesis gas also contains carbon dioxide, the volume fraction of which is preferably 15% or less, more preferably 11% or less. The synthesis gas prepared by the method can be used for preparing high-purity hydrogen or producing other downstream chemical products.
In the invention, the quenching water is quenched to obtain chilled ash water, and the method preferably further comprises the following steps of: and (3) cooling and depressurizing the chilled ash water in sequence, and filtering the chilled ash water, and then recycling the chilled ash water for quenching. In the invention, the temperature of chilled grey water is preferably 150-250 ℃, and the temperature of wastewater obtained after the cooling and depressurization treatment is preferably 40-50 ℃; the specific operation steps of the cooling and depressurization treatment are not particularly limited, and the operation steps well known to the person skilled in the art are adopted, and the cooling and depressurization treatment is particularly carried out in a 3-stage cooling and depressurization device so as to ensure that the obtained wastewater meets the requirements. In the present invention, the filtration is preferably mechanical filtration; the mechanical filtering process is not particularly limited, and the mechanical filtering process well known in the art is adopted to remove tiny particles in the wastewater; in the embodiment of the invention, the filtration is specifically filtration through a 200 mesh nylon filter cloth.
The entrained-flow gasification furnace is preferably a three-section furnace and comprises a high-temperature gasification device, a chilling water quenching device and a pressure-relief slag-discharging device, namely a high-temperature gasification section, a chilling water quenching section and a pressure-relief slag-discharging section which are respectively corresponding to the functions of the entrained-flow gasification furnace; the furnace type of the entrained-flow gasifier is preferably cylindrical, the material feed inlet of the entrained-flow gasifier is preferably positioned at the center of the top end of the high-temperature gasification device, and the furnace body lining of the high-temperature gasification device is sequentially provided with an insulating layer, a transition layer and a refractory layer from outside to inside; the heat-insulating layer is preferably made of rock wool; the material of the transition layer is preferably low-chromium refractory bricks; the refractory layer is preferably made of high-chromium refractory bricks; the high-temperature gasification device and the chilling water quenching device are preferably connected through a central pipe, namely a discharge hole at the bottom of the high-temperature gasification device is provided with a central pipe, the central pipe is led into the chilling water quenching device, a water film is formed on the inner wall of the central pipe, and the bottom of the central pipe is sealed in chilling water in the chilling water quenching device in a liquid mode; the high-temperature gasification device and the chilling water quenching device are preferably connected by a flange with water cooling; the chilling water quenching device and the pressure relief slag discharging device are preferably connected through a conventional flange. In the invention, after gasification reaction is carried out in the high-temperature gasification device, the obtained gas phase component and the molten phase component enter a chilling water quenching device through the central tube for chilling water quenching, and in the chilling water quenching process, a water film is formed on the inner wall of the central tube to prevent high-temperature substances from directly contacting the central tube, so that the high-temperature substances are heated and deformed; the gas phase component obtained after quenching of the quenching water escapes from the quenching water and is discharged, and the obtained solid slag is discharged into a pressure relief slag discharge device in an intermittent slag discharge mode.
FIG. 1 is a flow chart of a method for preparing synthesis gas by gasification of biomass entrained flow in an embodiment of the invention. As shown in figure 1, the invention comprises the steps of crushing solid rod-shaped biomass, dehydrating the crushed solid rod-shaped biomass, liquid biomass and powdery biomass together, grinding and screening to prepare biomass dry powder, conveying the biomass dry powder to an entrained flow gasifier, introducing oxygen, gasifying at high temperature in the presence of water vapor, quenching by chilled water, separating gas and liquid from the gas phase components, and performing gas phase washing and dust removal to obtain the biomass dry powder containing H 2 CO and CO 2 Is a synthesis gas of (2); cooling and depressurizing the chilled ash water obtained after chilled water quenching, filtering to remove solid slag, and recycling the chilled ash water as chilled water; and discharging the solid slag obtained after quenching by chilled water into a slag collecting tank.
The biomass energy conversion device uses the biomass dry powder as the raw material to carry out biomass resource utilization, and can realize high-efficiency conversion of biomass energy. Specifically, the method provided by the invention adopts a mode of combining spiral feeding and conveying with dense-phase pneumatic conveying in the conveying process of biomass dry powder, can effectively avoid the phenomena of strong water absorption and agglomeration of liquid organic slurry prepared from biomass, improves the biomass conveying amount of unit carrier gas, and makes up for the difficult problem of lower energy density of biomass itself. Compared with the traditional incineration method for treating biomass, the method can realize the efficient use of biomass materials, has no secondary pollution, and realizes the harmless utilization of biomass. The preparation of synthesis gas from biomass, and thus hydrogen from the synthesis gas, is an important route for the development of hydrogen energy. The biomass entrained-flow bed gasification technology provided by the invention can realize large-scale and continuous treatment of biomass and ensure continuous supply of hydrogen energy. The biomass gasification efficiency is higher by adopting the method, and the results of the examples show that the biomass gasification efficiency is more than or equal to 95%, and particularly 95-99%, according to the carbon material balance ((gas carbon content/total carbon content) multiplied by 100%).
The technical solutions of the present invention will be clearly and completely described in conjunction with the embodiments of the present invention, but they should not be construed as limiting the scope of the present invention.
Example 1
In the embodiment, the licorice traditional Chinese medicine fermentation residues are used as biomass raw materials, and are water-containing powdery materials (the water content is less than 45 wt%); placing the licorice traditional Chinese medicine fermentation residues in an oven, and drying for 1h at 105 ℃ so that the water content is 9wt%; grinding the dried materials in a grinding machine, and screening to obtain biomass dry powder with the granularity of less than 0.5 mm;
the biomass dry powder is conveyed to a high-temperature gasification device of an entrained flow gasification furnace in a mode of spiral feeding and conveying combined with dense-phase pneumatic conveying,the method comprises the following specific steps: the biomass dry powder is placed in a biomass bin, a low-pressure carrier gas (the carrier gas is carbon dioxide and the pressure is 1 MPa) is adopted to punch the biomass bin, so that the biomass dry powder is conveyed into a pressurizing bin, the pressurizing bin is closed by a stop valve and then is filled with the carrier gas to be pressurized, the pressure in the pressurizing bin after pressurization is 1.5MPa, a discharging valve of the pressurizing bin is opened, the biomass dry powder is conveyed into a charging hopper, a screw feeder is communicated with a discharging port at the bottom of the charging hopper, a material output pipe of the screw feeder is communicated with a feeding port of an entrained-flow gasification furnace, and in the process of conveying the biomass dry powder from the charging hopper to the screw feeder, the carrier gas (the pressure is 2.5 MPa) is added into the material output pipe of the screw feeder, so that the biomass dry powder is conveyed into a high-temperature gasification device, and the mass ratio of the biomass dry powder to the carrier gas is 140kg/m in the conveying process 3 The conveying flow of the biomass dry powder is 3t/h; while conveying the biomass dry powder, introducing superheated steam and oxygen preheated to 180 ℃ into the high-temperature gasification device, wherein the pressure of the superheated steam is 2.1MPa, and the oxygen conveying amount is 1500m 3 Carrying out gasification reaction for 10s at 1250 ℃ under the condition that the pressure in the high-temperature gasification device is 2MPa, so as to obtain a gas phase component and a molten state component;
the gas phase component and the molten phase component enter a quenching water quenching device through a central tube arranged at a discharge hole at the bottom of the high-temperature gasification device to be quenched, wherein in the quenching water quenching process, a water film is formed on the inner wall of the central tube, the bottom of the central tube is sealed in quenching water in the quenching water quenching device in a liquid way, and the flow rate of the quenching water is 20t/h; the gas phase component obtained after quenching water is escaped from the quenching water and discharged, and is subjected to gas-liquid separation in a cooling water separator and then is subjected to gas phase washing and dust removal in a washing tower by water to obtain synthesis gas; the temperature of the chilled ash water obtained after the chilled water quenching is 200 ℃, the temperature after the treatment by a 3-stage cooling and depressurization device is 60 ℃, and the chilled ash water is circularly recycled to be used as chilled water after the filtration treatment by a 200-mesh nylon filter cloth; the solid slag obtained after quenching water is discharged into a pressure relief slag discharging device in an intermittent slag discharging mode.
The synthesis gas prepared in this example was analyzed by a gas composition analyzer, and it was shown that the volume fraction of hydrogen, the volume fraction of carbon monoxide and the volume fraction of carbon dioxide in the synthesis gas were 42%, 41% and 15%. Meanwhile, according to the carbon material balance ((gas carbon content/total carbon content) ×100%) the biomass gasification efficiency was calculated to be 98%.
Comparative example 1
Synthesis gas was prepared as in example 1, except that in this comparative example, a separate screw feed transfer was used to transfer the biomass dry powder.
The synthesis gas prepared in this comparative example was analyzed by a gas composition analyzer, and the results showed that the volume fraction of hydrogen, the volume fraction of carbon monoxide and the volume fraction of carbon dioxide in the synthesis gas were 40%, 38% and 20%. Meanwhile, according to the carbon material balance ((gas carbon content/total carbon content) ×100%) the biomass gasification efficiency was calculated to be 95%.
Comparative example 2
Synthesis gas was prepared as in example 1, except that in this comparative example, a separate dense phase pneumatic transport mode was used to transport the biomass dry powder.
The synthesis gas prepared in this comparative example was analyzed by a gas composition analyzer, and it was shown that the volume fraction of hydrogen, the volume fraction of carbon monoxide and the volume fraction of carbon dioxide in the synthesis gas were 37%, 36% and 23%. Meanwhile, according to the carbon material balance ((gas carbon content/total carbon content) ×100%) the biomass gasification efficiency was calculated to be 90%.
Example 2
In the embodiment, the fritillaria thunbergii fruit particles are used as biomass raw materials, the fritillaria thunbergii fruit particles are oily fruit biomass, and the water content is 40wt%; roasting 10t of the fritillary fruit particles at 200 ℃ for 3 hours to obtain roasted fritillary particles (the physicochemical properties of the roasted fritillary fruit particles are shown in table 1); placing the baked fritillary bulb particles into a pulverizer for pulverizing, sieving with a sieve with the diameter of 0.25mm, and collecting undersize part as biomass dry powder (5.4 t);
TABLE 1 physicochemical Properties of calcined Bulbus Fritillariae Thunbergii particles
The biomass dry powder is conveyed to a high-temperature gasification device of an entrained flow gasification furnace in a mode of spiral feeding and conveying combined with dense-phase pneumatic conveying, and the method comprises the following specific steps: the biomass dry powder is placed in a biomass bin, a low-pressure carrier gas (the carrier gas is carbon dioxide and the pressure is 0.4 MPa) is adopted to punch the biomass bin, so that the biomass dry powder is conveyed into a pressurizing bin, the pressurizing bin is closed by a stop valve and then is filled with the carrier gas to be pressurized, the pressure in the pressurizing bin after pressurization is 1.6MPa, a discharge valve of the pressurizing bin is opened, the biomass dry powder is conveyed into a feeding hopper, a screw feeder is communicated with a discharge outlet at the bottom of the feeding hopper, a material output pipe of the screw feeder is communicated with a feed inlet of the entrained-flow gasifier, and in the process of conveying the biomass dry powder from the feeding hopper to the screw feeder, the carrier gas (the pressure is 2 MPa) is additionally added into a material output pipe of the screw feeder, so that the biomass dry powder is conveyed into a high-temperature gasification device, and the mass ratio of the biomass dry powder to the carrier gas is 165kg/m in the conveying process 3 The conveying flow of the biomass dry powder is 1t/h; while conveying the biomass dry powder, introducing superheated steam and oxygen preheated to 180 ℃ into the high-temperature gasification device, wherein the pressure of the superheated steam is 2MPa (the conveying amount of the superheated steam is 300m 3 And/h), oxygen transport of 600m 3 Carrying out gasification reaction for 10s at 1300 ℃ under the pressure of 2.5MPa in the high-temperature gasification device to obtain a gas phase component and a molten phase component;
the gas phase component and the molten phase component enter a quenching water quenching device through a central tube arranged at a discharge hole at the bottom of the high-temperature gasification device to be quenched, wherein in the quenching water quenching process, a water film is formed on the inner wall of the central tube, the bottom of the central tube is sealed in quenching water in the quenching water quenching device in a liquid way, and the flow rate of the quenching water is 10t/h; the gas phase component obtained after quenching water is escaped from the quenching water and discharged, and is subjected to gas-liquid separation in a cooling water separator and then is subjected to gas phase washing and dust removal in a washing tower by water to obtain synthesis gas; the temperature of the chilled ash water obtained after the chilled water quenching is 200 ℃, the temperature after the treatment by a 3-stage cooling and depressurization device is 60 ℃, and the chilled ash water is circularly recycled to be used as chilled water after the filtration treatment by a 200-mesh nylon filter cloth; the solid slag obtained after quenching water is discharged into a pressure relief slag discharging device in an intermittent slag discharging mode.
The synthesis gas prepared in this example was analyzed by a gas composition analyzer, and the results showed that the volume fraction of hydrogen, the volume fraction of carbon monoxide and the volume fraction of carbon dioxide in the synthesis gas were 42%, 43% and 11%. Meanwhile, according to the carbon material balance ((gas carbon content/total carbon content) ×100%) the biomass gasification efficiency was calculated to be 99%.
Comparative example 3
Synthesis gas was prepared as in example 2, except that in this comparative example, a separate dense phase pneumatic transport mode was used to transport the biomass dry powder.
The synthesis gas prepared in this comparative example was analyzed by a gas composition analyzer, and it was shown that the volume fraction of hydrogen, the volume fraction of carbon monoxide and the volume fraction of carbon dioxide in the synthesis gas were 40%, 42% and 12%. Meanwhile, according to the carbon material balance ((gas carbon content/total carbon content) ×100%) the biomass gasification efficiency was calculated to be 95%.
Comparative example 4
In the comparative example, fritillaria thunbergii fruit particles are used as biomass raw materials, synthesis gas is prepared by gasifying the fritillaria thunbergii fruit particles by adopting a fixed bed, equipment used is a straight-tube type fixed bed gasifier, gasification reaction is carried out under the condition of air, the air is conveyed into the fixed bed gasifier in a lower air inlet mode, and the conveying amount is 1000m 3 /h；
The fritillary fruit particles are fed from the upper part of the fixed bed gasifier, sequentially enter a drying zone 180 ℃, a pyrolysis zone 500 ℃, an oxidation zone 900 ℃ and a reduction zone 1020 ℃ for treatment (the total treatment time is 6 s), and synthesis gas is obtained; the fritillary fruit particles are treated by adopting intermittent filler, and the adding amount is 500kg/h.
The synthesis gas prepared in this comparative example was analyzed by a gas composition analyzer, and the results showed that the volume fraction of hydrogen, the volume fraction of carbon monoxide and the volume fraction of carbon dioxide in the synthesis gas were 17%, 20% and 15%. Meanwhile, according to the carbon material balance ((gas carbon content/total carbon content) ×100%) the biomass gasification efficiency was calculated to be 83%. The volume fraction of the active gas component in the synthesis gas of this comparative example was 37%, because air was used as the oxidizing gas in the gasification process, and 78% of nitrogen was contained in the air, resulting in incomplete gasification, and the gasification efficiency of biomass was lower than that of comparative example 3.
According to the embodiment and the comparative example, the biomass dry powder is used as the raw material, and the biomass dry powder is conveyed to the entrained-flow gasifier by adopting a conveying mode of combining spiral feeding conveying with dense-phase pneumatic conveying, so that compared with the existing gasification mode, the gasification efficiency and the yield of the synthesis gas are improved.
Although the foregoing embodiments have been described in some, but not all, embodiments of the invention, according to which one can obtain other embodiments without inventiveness, these embodiments are all within the scope of the invention.
Claims (10)
1. The method for preparing the synthesis gas by gasifying the biomass entrained-flow bed is characterized by not adopting pulverized coal or coal water slurry and comprises the following steps of:
conveying biomass dry powder into an entrained flow gasifier in a spiral feeding and conveying mode, and carrying out gasification reaction under the condition of oxygen and water vapor to obtain the synthesis gas;
and dense-phase pneumatic conveying is accompanied in the spiral feeding conveying process.
2. The method of claim 1, wherein the dry biomass powder has a particle size of 0.5mm or less and a water content of 10wt% or less.
3. A method according to claim 1 or 2, wherein the carrier gas used for dense phase pneumatic transport is carbon dioxide or nitrogen.
4. The method according to claim 3, wherein the pressure of the carrier gas in the conveying process is 2-6 MPa, and the ratio of the mass of the biomass dry powder to the volume of the carrier gas is more than or equal to 100kg/m 3 。
5. The method according to claim 1, wherein the mass ratio of the volume of oxygen to the biomass dry powder is 400-700 m 3 :1t; the pressure of the water vapor is 2-6 MPa.
6. The method according to claim 1 or 5, wherein the gasification reaction is carried out at a temperature of 1000-1600 ℃, a pressure of 0.5-5 mpa, and a time of 4-12 s.
7. The method of claim 1, wherein the gasification reaction further results in a molten component, and wherein the gasification reaction further comprises, after the gasification reaction: and (3) quenching the gas phase component and the molten phase component obtained by the gasification reaction by adopting a water cooling mode to obtain synthesis gas and solid slag respectively.
8. The method of claim 7, wherein the flow rate of the chilled water used for the chilled water quench is 6-10 times the biomass dry powder delivery flow rate.
9. The method according to claim 7 or 8, wherein the quenching of the chilled water further yields chilled grey water, further comprising, after the chilled grey water is obtained: and (3) cooling and depressurizing the chilled ash water in sequence, and filtering the chilled ash water, and then recycling the chilled ash water for quenching.
10. The method according to claim 7 or 8, wherein the chilled water quench further comprises: and (3) performing gas phase washing and dust removal on gas phase components obtained after quenching water by gas-liquid separation to obtain synthesis gas.
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