CN116478736A - System and method for preparing synthesis gas by biomass thermal conversion - Google Patents
System and method for preparing synthesis gas by biomass thermal conversion Download PDFInfo
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- CN116478736A CN116478736A CN202210038284.8A CN202210038284A CN116478736A CN 116478736 A CN116478736 A CN 116478736A CN 202210038284 A CN202210038284 A CN 202210038284A CN 116478736 A CN116478736 A CN 116478736A
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- 239000002028 Biomass Substances 0.000 title claims abstract description 82
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 51
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 51
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 38
- 238000000034 method Methods 0.000 title claims abstract description 36
- 239000007789 gas Substances 0.000 claims abstract description 152
- 238000000197 pyrolysis Methods 0.000 claims abstract description 78
- 239000001301 oxygen Substances 0.000 claims abstract description 52
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 52
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000002245 particle Substances 0.000 claims abstract description 48
- 239000002994 raw material Substances 0.000 claims abstract description 48
- 238000002309 gasification Methods 0.000 claims abstract description 38
- 239000000571 coke Substances 0.000 claims abstract description 37
- 238000002407 reforming Methods 0.000 claims abstract description 27
- 238000005336 cracking Methods 0.000 claims abstract description 13
- 230000009471 action Effects 0.000 claims abstract description 12
- 239000012071 phase Substances 0.000 claims description 39
- 239000007787 solid Substances 0.000 claims description 31
- 238000010438 heat treatment Methods 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 238000002485 combustion reaction Methods 0.000 claims description 15
- 238000002156 mixing Methods 0.000 claims description 15
- 230000009467 reduction Effects 0.000 claims description 15
- 238000010517 secondary reaction Methods 0.000 claims description 13
- 239000000463 material Substances 0.000 claims description 12
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- 239000001257 hydrogen Substances 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 10
- 238000004519 manufacturing process Methods 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 7
- 229910001882 dioxygen Inorganic materials 0.000 claims description 7
- 230000035484 reaction time Effects 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 5
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 239000007790 solid phase Substances 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 239000000047 product Substances 0.000 description 50
- 239000003570 air Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 238000000354 decomposition reaction Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 238000009826 distribution Methods 0.000 description 4
- 239000000428 dust Substances 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 230000035515 penetration Effects 0.000 description 4
- 239000010902 straw Substances 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000000465 moulding Methods 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 239000012808 vapor phase Substances 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 238000011065 in-situ storage Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000003908 quality control method Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N silicon dioxide Inorganic materials O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- 241000209140 Triticum Species 0.000 description 1
- 235000021307 Triticum Nutrition 0.000 description 1
- 240000008042 Zea mays Species 0.000 description 1
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 1
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 235000013339 cereals Nutrition 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 235000005822 corn Nutrition 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229920005610 lignin Polymers 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000003039 volatile agent Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/12—Heating the gasifier
- C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention discloses a system and a method for preparing synthesis gas by biomass thermal conversion, wherein the system comprises the following steps: a feeding unit for providing biomass raw materials of two different-size particles and alternately feeding the biomass raw materials; the cavity of the microwave pyrolysis unit is in an inner sleeve and an outer sleeve structure, and two biomass raw materials form moving bed layers which are alternately distributed along the axial direction in the inner sleeve; oxygen enters from the upper part of a space between the inner sleeve and the outer sleeve and flows along the radial direction at the middle lower part of the inner sleeve, the biomass raw material is heated by microwaves and is subjected to aerobic pyrolysis, and the generated gas-phase product flows out from a gas-phase channel extending along the axis of the inner sleeve. The invention can obviously improve the quality of gas phase products through the feeding unit and the microwave pyrolysis unit, creates conditions for obtaining the final synthetic product gas with higher quality, and can solve the problem of microwave energy consumption. The product gas quality can be further improved through the combined action of the solid-state bio-coke gasification unit and the gaseous volatile component cracking reforming unit.
Description
Technical Field
The invention relates to the technical field of biomass energy utilization, in particular to a system and a method for preparing synthesis gas by biomass thermal conversion.
Background
Biomass mainly refers to lignocellulose (lignin for short) such as straw, trees and the like except grains and fruits in the agriculture and forestry production process. The preparation of combustible gases such as fuel gas, synthesis gas, hydrogen, methane and the like by using biomass is an important way for realizing the value-added utilization of biomass. The existing biomass gas fuel preparation method comprises a fixed bed, a fluidized bed, an entrained flow, a plasma and microwave gasification method and the like, wherein the method for gasifying biomass by utilizing microwaves can enable energy to rapidly act inside the biomass, so that the energy transmission loss existing in conventional heating is radically overcome, the method has the advantages of high heating rate, high energy utilization efficiency, small thermal inertia and the like, and from the distribution composition of products, gas products have combustible components such as hydrogen, carbon monoxide, methane and the like with higher concentration, can be directly or further processed and used as chemical raw materials such as synthetic gas, hydrogen and the like and new energy sources, and have good application prospects.
The existing microwave pyrolysis gasification system has the following technical problems: under the action of no exogenous reactive gas, it is difficult to obtain high-yield synthesis gas by virtue of the decomposition of biomass alone; the inside and outside of the microwave reactor are heated unevenly, and the pyrolysis efficiency is limited; in the process of preparing the synthetic gas, the processes of microwave pyrolysis, biological oil gas pyrolysis reforming, biological coke gasification and the like are overlapped together, and tar carried by gas is difficult to be removed. The dust removal effect is poor; the microwave energy consumption is higher, and the condition that the heating efficiency is not high due to insufficient installed microwave power exists.
Chinese patent application CN105524662a discloses a method for producing synthesis gas by microwave pyrolysis gasification of biomass. The scheme comprises the following contents: biomass raw materials and catalysts fed into a storage bin enter a microwave pyrolysis reactor to sequentially pass through a preheating zone, a pyrolysis zone, a gasification zone and a reforming zone for dehydration, pyrolysis, gasification and reforming reactions, products after reforming are subjected to gas-solid separation, wherein gas and a small amount of tar and coke carried in the gas are subjected to pyrolysis reaction again in a gas lifting pipe, synthetic gas is released from an outlet, and coke and ash obtained by gas-solid separation are discharged out of the reactor. Although the method realizes higher biomass gasification rate and effectively improves the quality of the synthetic gas product, the problem of microwave energy consumption is not solved, and the temperature in the middle of the reactor cannot be ensured.
Therefore, a system and a method for preparing synthesis gas by biomass thermal conversion, which can not only remarkably improve the quality of product gas, but also solve the problem of microwave energy consumption, are needed.
The information disclosed in this background section is only for enhancement of understanding of the general background of the invention and should not be taken as an acknowledgement or any form of suggestion that this information forms the prior art already known to a person of ordinary skill in the art.
Disclosure of Invention
The invention aims to provide a system and a method for preparing synthesis gas by biomass thermal conversion, which can not only remarkably improve the quality of gas-phase products by a feeding unit and a microwave pyrolysis unit and create better conditions for obtaining the final synthesis product gas with higher quality, but also solve the problem of microwave energy consumption.
Another object of the present invention is to further enhance the product gas quality by the combined action of the solid-state bio-char gasification unit and the gaseous volatile component cracking reforming unit.
To achieve the above object, according to a first aspect of the present invention, there is provided a system for producing synthesis gas by thermal conversion of biomass, comprising: a feeding unit for providing biomass raw materials of two different-size particles and alternately feeding the biomass raw materials; the cavity of the microwave pyrolysis unit is in an inner sleeve and an outer sleeve structure, and two biomass raw materials form moving bed layers which are alternately distributed along the axial direction in the inner sleeve; oxygen enters from the upper part of a space between the inner sleeve and the outer sleeve and flows along the radial direction at the middle lower part of the inner sleeve, the biomass raw material is heated by microwaves and is subjected to aerobic pyrolysis, and the generated gas-phase product flows out from a gas-phase channel extending along the axis of the inner sleeve.
Further, in the above technical solution, the feeding unit may include: the parallel double bins are respectively provided with biomass raw materials of the two particles with different sizes; the inlet end of the material conveying screw is respectively communicated with the double bins through Y-shaped pipelines, and the outlet end of the material conveying screw is communicated with the inner sleeve of the microwave pyrolysis unit.
Further, in the above technical scheme, the microwave pyrolysis unit further comprises a microwave generator, which can be arranged outside the wall of the outer sleeve and uniformly arranged along the circumferential direction of the outer wall of the outer sleeve.
In the technical scheme, the wall surface of the middle lower part of the inner sleeve can be provided with oxygen holes for oxygen to flow out radially; the middle and lower walls and the bottom of the gas phase channel can be provided with gas phase product pores.
In the technical scheme, the wall surface height of the oxygen gas hole can be 30% -60% of the whole height of the inner sleeve, and the aperture of the oxygen gas hole is 0.5-5 mm; the wall surface height of the gas phase product air hole can be 1/3-2/3 of the whole height of the gas phase channel, the aperture of the gas phase product air hole is 0.2-2 mm, and the aperture ratio is 10-30%.
Further, in the above technical solution, the gas phase product generated by the microwave pyrolysis unit is a gaseous volatile component, and the system of the present invention further includes: the gaseous volatile component cracking reforming unit is arranged at the upper part of the entrained flow bed and is provided with a throat structure, a nozzle which is circumferentially arranged along the entrained flow bed and radially extends is arranged in the throat area, and a multi-gas-path annular channel and a cyclone mixing channel are arranged in the nozzle and are used for introducing oxygen and water vapor and carrying out cracking reforming on the gaseous volatile component.
Further, in the above technical solution, the multi-gas-path annular channel may include: an inner ring channel which is arranged at the innermost side and is filled with oxygen; the middle ring channel is arranged at the outer side of the inner ring channel and is filled with gaseous volatile matters; and the outer ring channel is arranged at the outer side of the middle ring channel and is filled with water vapor.
Furthermore, in the technical scheme, the rotational flow mixing channel can be arranged into a cone structure, and the included angle between the inclined plane of the cone and the bottom surface is 20-70 degrees.
The system of the present invention may further comprise: the solid bio-coke gasification unit is arranged at the lower part of the entrained flow and receives solid bio-coke from the cavity of the microwave pyrolysis unit through a bio-coke conveying screw; the solid bio-coke gasification unit is provided with a combustion zone into which oxygen is introduced and a reduction zone into which water vapor is introduced; and the gasified product rises to enter a throat area for secondary reaction to obtain product gas.
Further, in the above technical scheme, a fire grate can be arranged between the combustion zone and the reduction zone; and a gas distributor which is obliquely arranged is arranged below the fire grate and at the corresponding position of the water vapor inlet.
According to a second aspect of the present invention there is provided a process for the production of synthesis gas by thermal conversion of biomass comprising the steps of: A. forming alternate feeding of the pretreated biomass raw materials with two different-size particles; B. while heating the biomass raw material by microwaves, performing aerobic pyrolysis by radially flowing oxygen; C. and leading out the generated gaseous volatile matters from a gas phase channel which is arranged along the axis of the inner sleeve of the microwave pyrolysis unit.
Further, in the above technical solution, step B may further include: b1, forming cross flow by the radially flowing oxygen and the axially downward moving solid-phase biomass raw material for dedusting gas-phase products; aerobic pyrolysis supplies heat for microwave reaction, and the generated heat is transferred to the axle center through radial airflow; b2, forming a large-particle low-temperature region and a small-particle high-temperature region in the microwave field, wherein the small-particle high-temperature region is pyrolyzed to generate oil gas, the oil gas flows to the large-particle low-temperature region with smaller air resistance, and heavy component tar in the oil gas is condensed and adhered to the large-particle low-temperature region in the flowing process.
Further, in the above technical solution, the biomass raw material in the step a may be a lignocellulose-containing material; the pretreatment may include air drying, pulverizing, and molding.
Further, in the above technical scheme, the microwave heating reaction time can be 5-20 minutes, and the microwave power density is 0.1×10 5 ～1×10 5 W/m 3 The method comprises the steps of carrying out a first treatment on the surface of the In the presence of aerobic pyrolysis, the temperature of the axial center area of the inner sleeve can reach 400-600 ℃, and the temperature of the circumferential area of the cylinder wall can reach 600-800 ℃; the temperature of the small particle high temperature area is 50-100 ℃ higher than that of the large particle low temperature area.
The method of the present invention may further comprise: D. introducing solid bio-coke generated by microwave aerobic pyrolysis into a gasification unit, and generating a gas-phase product rich in synthesis gas under the combined action of oxygen and steam; E. introducing the gaseous volatile matters generated in the step C into a cracking reforming unit, forming multi-gas-path rotational flow mixing of the gaseous volatile matters, oxygen and water vapor in a throat area, and performing primary reaction; and D, enabling the gas phase product rich in the synthesis gas generated in the step to enter a throat area and performing secondary reaction at a high temperature state to obtain the synthesis gas product.
In the technical scheme, the solid-state bio-coke gasification unit is provided with a combustion zone and a reduction zone, wherein the temperature of the combustion zone is 900-1200 ℃, and the temperature of the reduction zone is 800-1000 ℃; the reaction time of the solid biological coke gasification unit is 5-20 minutes.
Further, in the above technical scheme, the primary reaction conditions in step E may be: oxygen flow rate is 0.5-5 m 3 And/h, the flow rate of the water vapor is 0.5-5 m 3 /h; the secondary reaction temperature can be 1000-1200 ℃.
Furthermore, in the above technical scheme, the synthesis gas product in step E is rich in hydrogen and carbon monoxide, and the ratio of hydrogen to carbon monoxide is between 1.5 and 3.0; carbon dioxide content less than 25%, tar content less than 1mg/Nm 3 Ash content of not more than 10mg/Nm 3 The gas yield in the whole process is not lower than 2.5Nm 3 /kg of dry biomass.
Compared with the prior art, the invention has the following beneficial effects:
1) According to the invention, oxygen is introduced into the microwave pyrolysis unit, so that heat supply is realized in a mode of combining the aerobic pyrolysis and the microwave heating, and after the oxygen is introduced into the microwave field, the oxidation reaction is exothermic, so that heat supply can be supplemented for the reaction; meanwhile, the generated heat is radially transferred to the axle center by the air flow, so that radial heat transfer is enhanced, especially the temperature of the axle center area of the inner sleeve is reinforced, the temperature of the integral bed layer is also raised, and complete pyrolysis of biomass is promoted. Not only can obviously reduce microwave energy consumption, but also can strengthen the quality improvement of the radial flow process of gas and the gasification efficiency of biological coke; meanwhile, compared with the conventional biomass gasification technology, the method can obviously reduce oxygen consumption and improve the hydrogen-carbon ratio and component regulation of the gas product.
2) According to the invention, a mode of alternately feeding large and small particles is adopted to form double particle layer distribution in a microwave pyrolysis unit, the characteristic of differential heating of the microwaves on particles with different sizes is utilized, a large particle low-temperature region and a small particle high-temperature region are formed in a microwave field, the small particle high-temperature region is pyrolyzed for generating oil gas, the oil gas flows to the large particle low-temperature region with smaller air resistance more easily, and the large particle bed region synchronously forms a gas channel, so that the flow resistance of pyrolysis gas phase products is reduced to the maximum extent, the damage of light components is avoided, and the selective pyrolysis on heavy components is realized; heavy component tar in oil gas can be condensed and adhered to a large-particle low-temperature area in the flowing process, and the radial flow of air flow and the axial flow of solid-phase materials form a cross flow effect, so that the gas dust removal effect is achieved, the oil gas can be purified more effectively, and the quality and the yield of the oil gas can be remarkably improved.
3) The microwave pyrolysis can obtain gaseous volatile matters with higher quality, thereby creating conditions for generating the synthesis product gas with higher quality subsequently. The tar carried by the gas can be removed more effectively by coupling and integrating the processes of microwave pyrolysis, solid bio-coke gasification, gaseous volatile component cracking reforming and the like; the gaseous volatilization splitting decomposition reforming unit adopts the nozzle which is arranged in the throat area and provided with a plurality of gas paths of annular channels and a rotational flow mixing channel, so that the uniform mixing of gases can be ensured, and the blockage of the nozzle can be effectively avoided. The solid biological coke gasification unit and the gaseous volatile split decomposition reforming unit are communicated in the entrained flow so as to realize primary reaction and secondary reaction in the throat area, ensure the heat value of raw materials and further realize the acquisition of high-quality synthetic product gas.
The foregoing description is only an overview of the present invention, and it is to be understood that it is intended to provide a more clear understanding of the technical means of the present invention and to enable the technical means to be carried out in accordance with the contents of the specification, while at the same time providing a more complete understanding of the above and other objects, features and advantages of the present invention, and one or more preferred embodiments thereof are set forth below, together with the detailed description given below, along with the accompanying drawings.
Drawings
FIG. 1 is a schematic diagram of a system for producing synthesis gas by thermal conversion of biomass according to the present invention.
FIG. 2 is a schematic diagram of the configuration of the nozzle in the throat area of the gaseous volatile cracking reforming unit in the system of the present invention.
The main reference numerals illustrate:
1-a feeding unit, 11-a first bin, 12-a second bin, 13-a Y-type conveying pipe and 14-a first conveying screw;
2-microwave pyrolysis unit, 20-microwave generator, 21-outer sleeve, 22-inner sleeve, 23-oxygen inlet, 24-gas phase channel, 25-gaseous volatile outlet, 26-second feeding screw;
3-solid bio-coke gasification unit, 31-oxygen inlet, 32-grate, 33-gas distributor, 34-steam inlet;
4-gaseous volatile component cracking reforming unit, 41-throat area, 42-nozzle, 42A-multi-gas-path annular channel, 42A-inner annular channel, 42B-middle annular channel, 42 c-outer annular channel, 42B-rotational flow mixing channel, 43-synthetic product gas outlet.
Detailed Description
The following detailed description of embodiments of the invention is, therefore, to be taken in conjunction with the accompanying drawings, and it is to be understood that the scope of the invention is not limited to the specific embodiments.
Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations thereof such as "comprises" or "comprising", etc. will be understood to include the stated element or component without excluding other elements or other components.
Spatially relative terms, such as "below," "beneath," "lower," "above," "upper," and the like, may be used herein for ease of description to describe one element's or feature's relationship to another element's or feature's in the figures. It will be understood that the spatially relative terms are intended to encompass different orientations of the article in use or operation in addition to the orientation depicted in the figures. For example, if the article in the figures is turned over, elements described as "below" or "beneath" other elements or features would then be oriented "above" the elements or features. Thus, the exemplary term "below" may encompass both a direction of below and a direction of above. The article may have other orientations (rotated 90 degrees or other orientations) and the spatially relative descriptors used herein interpreted accordingly.
The terms "first," "second," and the like herein are used for distinguishing between two different elements or regions and are not intended to limit a particular position or relative relationship. In other words, in some embodiments, the terms "first," "second," etc. may also be interchanged with one another.
The inventors have found that: according to the special rule that the penetration depth of microwaves is reduced along with the enhancement of the wave absorbability of the medium, the penetration depth of microwaves caused by temperature rise is gradually reduced when the large-volume biomass is heated by microwaves, and the common problems of uneven heating inside and outside materials, limited pyrolysis efficiency, low gas quality control and the like are easily caused. Further, the microwave heat and mass transfer isotropy easily generates intermediate components including tar and light hydrocarbon; the dielectric heating characteristic of microwaves is characterized in that the biomass with poor wave absorption is difficult to heat and the reflection loss of microwave energy is high, and the bio-coke with strong wave absorption is too fast to heat and easy to overheat, and the process control difference is large before and after the reaction; biomass itself lacks an effective decarbonization heating factor and the pyrolysis process is not feasible by means of microwave energy alone.
Based on the above study, as shown in fig. 1, the present invention provides a system for producing synthesis gas by thermal conversion of biomass. The system comprises a feeding unit 1 and a microwave pyrolysis unit 2, and can remarkably improve the quality of gas-phase products, create better conditions for obtaining final synthetic product gas with higher quality and solve the problem of microwave energy consumption. The system can also comprise a solid-state bio-coke gasification unit 3 and a gaseous volatile decomposition reforming unit 4, and the product gas quality is further improved through the combined action of the solid-state bio-coke gasification unit and the gaseous volatile decomposition reforming unit.
As further shown in fig. 1, a feed unit 1 is provided for providing biomass feedstock of two different size particles and alternately feeding. Specifically, the feeding unit further comprises a parallel double-bin and a first conveying screw 14, wherein the parallel double-bin comprises a first bin 11 and a second bin 12, and biomass raw materials with two different-size particles are respectively arranged in the two bins. The biomass raw material can be derived from corn straw, rice husk, wheat straw, wood block, tree leaf or branch and any substances containing lignocellulose, and can be pretreated before entering the feeding unit, and the biomass raw material with small density and small requirement for forming of the straw is subjected to the pretreatment process comprising the following steps of airing, crushing and forming: directly crushing the dried biomass to below 2mm, and then physically extruding and forming under the condition of 10-20 MPa to obtain a biomass raw material; the biomass raw material with large density and no need of molding is directly cut into the biomass raw material with the size close to the molding size. The inlet end of the first material conveying screw 14 is respectively communicated with the two bins through a Y-shaped pipeline, a star-shaped valve is arranged on the pipeline, and the outlet end of the first material conveying screw 14 is communicated with the inner sleeve of the microwave pyrolysis unit 2 and is used for alternately conveying biomass raw materials with two different diameters for the microwave pyrolysis unit 2.
As further shown in fig. 1, the cavity of the microwave pyrolysis unit 2 is of an inner and outer sleeve structure (comprising an outer sleeve 21 and an inner sleeve 22), and two biomass raw materials form moving bed layers which are alternately distributed along the axial direction in the inner sleeve due to alternate feeding. Wherein the height ratio of the small-size raw material bed layer to the large-size raw material bed layer can be 1:0.1-0.5, the particle size of the small-size raw material is 6-20 mm, and the particle size of the large-size raw material is 40-100 mm. The alternate arrangement of the two ruler-diameter raw material layers is beneficial to changing the original reaction path of microwave pyrolysis and promoting the process efficiency and the quality improvement of pyrolysis products. Preferably, but not limited to, the wall surface of the middle lower part of the inner sleeve 22 is provided with oxygen gas holes for oxygen to flow out radially, the oxygen gas holes can be distributed in multiple layers along the axial direction, the number of distribution layers can be 4-10, each layer is uniformly distributed along the circumference of the cylinder wall, the number of each layer is 6-60, the height of the distribution layer of the oxygen gas holes can be 30-60% of the height of the inner sleeve, and the pore diameter of the air holes is 0.5-5 mm. Oxygen enters from the upper part of the space between the inner sleeve and the outer sleeve (namely the oxygen inlet 23 in fig. 1) and flows along the radial direction at the lower part of the inner sleeve, and the flow direction is the circumference of the cylinder wall to the axis. Simultaneously, the biomass raw material moves downwards along the axial direction under the action of gravity to form cross flow with oxygen flowing in the radial direction, and microwaves are generatedWhile heating the biomass feedstock, the biomass feedstock undergoes aerobic pyrolysis, and the resulting vapor phase product flows upwardly from a vapor phase passage 24 extending along the axis of the inner sleeve 22 and out of a vapor phase volatile outlet 25. The heterogeneous cross flow formed is beneficial to the dust removal of gas-phase products, and because the oxidation reaction is an exothermic reaction, the generated heat is transferred to the axle center through radial air flow in the radial flow process of oxygen, and the temperature loss of microwave heating in the axle center area is compensated, namely, the combination of aerobic pyrolysis and microwave heating is realized under the participation of the radial flow of oxygen. In addition, because of alternate feeding, the moving bed is a bed layer with large and small particles alternately distributed along the axial direction, a large particle low-temperature region and a small particle high-temperature region can be formed in a microwave field, the small particle high-temperature region is pyrolyzed for generating oil gas, the oil gas flows to the large particle low-temperature region with smaller air resistance, and heavy component tar in the oil gas is condensed and adhered to the large particle low-temperature region in the flowing process, so that a cleaner gas-phase product can be obtained. As further shown in fig. 1, gas product gas holes are formed in the lower wall surface and the bottom of the gas phase passage 24, the pore diameter of the gas holes can be 0.2-2 mm, the aperture ratio can be 10-30%, and the height of the aperture area is 1/2-4/5 of the height of the inner sleeve 22. The microwave generators 20 used in the microwave pyrolysis unit 2 are disposed outside the wall of the outer sleeve 21 and are uniformly arranged along the circumferential direction of the outer wall of the outer sleeve 21. Specifically, the cavities of the microwave pyrolysis unit 2 are respectively provided with a certain number of microwave quartz windows, each window corresponds to one microwave generator 20, the power of a single microwave generator can be 500-2000W, the number of the specific windows is set according to the volume of the reactor and the like, and generally 2-10 windows are set, so that the power density in the reaction cavity is ensured to be 0.1×10 5 ～2×10 5 W/m 3 。
As further shown in fig. 1, the solid bio-char gasification unit 3 is disposed at the lower portion of the entrained flow bed 30 and receives the solid bio-char from the bottom of the cavity of the microwave pyrolysis unit 2 through a bio-char conveying screw (i.e., the second feed screw 26 in fig. 1). The solid biocoke gasification unit 3 is provided with a combustion zone into which the working gas 1 is introduced and a reduction zone into which the working gas 2 is introduced. The working gas 1 is mainly oxygen (see oxygen inlet 31 in FIG. 1), and can be a mixture of oxygen, air, oxygen and nitrogenPreferably, a mixed gas of oxygen and nitrogen is used, wherein the mixing ratio of oxygen and nitrogen is 1:0.05 to 0.5, and the flow is controlled to be 0.1 to 1m 3 /h; the working gas 2 is mainly steam (see steam inlet 34 in FIG. 1) and is one of steam, carbon dioxide and their mixture, preferably steam, and the flow rate is controlled to be 0.05-0.5 m 3 And/h. The temperature of the combustion zone is 900-1200 ℃, and the temperature of the reduction zone is 800-1000 ℃; the reaction time in the solid bio-coke gasification unit is 5-20 minutes. As further shown in FIG. 1, a grate 32 is disposed between the combustion zone and the reduction zone, and a gas distributor 33 is disposed below the grate 32 at a location corresponding to the steam inlet 34. The gas distributor 33 may be any one of a sieve-hole type, a pipeline type, a grid type, and the like; the grate 32 may be any of a fixed grate, a reciprocating grate, a vibrating grate, a rotating grate, etc., and the powdered ash may be discharged by controlling the operating frequency of the grate. The product of the gasification of the solid bio-coke in the combustion zone and the reduction zone rises into the gaseous volatile split reforming unit 4 of the invention.
As further shown in fig. 1, the solid bio-coke gasification unit 3 is directly communicated with the gaseous volatile decomposition reforming unit 4, a throat area 41 is arranged at the upper part of the gaseous volatile decomposition reforming unit 4, a plurality of nozzles 42 are arranged in the throat area 41, the nozzles 42 are uniformly distributed along the circumference of the entrained flow bed 30, the number of the nozzles is 3-20, and the nozzles 42 face the direction of the circle center of the entrained flow bed 30. The top of the gaseous volatile component cracking reforming unit 4 is provided with a synthesis product gas outlet 43. As further shown in fig. 2, a multi-gas path annular channel 42A and a swirl mixing channel 42B are provided in the nozzle 42 for introducing oxygen and water vapor and for cracking and reforming gaseous volatiles. Specifically, the multi-gas-path annular channel 42A includes an inner annular channel 42A, an intermediate annular channel 42B and an outer annular channel 42c, the inner annular channel 42A is arranged at the innermost side and is filled with oxygen, the intermediate annular channel 42B is arranged at the outer side of the inner annular channel and is filled with gaseous volatile matters from the microwave pyrolysis unit 2, the outer annular channel 42c is arranged at the outer side of the intermediate annular channel and is filled with water vapor, the outlets of the channels are communicated with a rotational flow mixing channel 42B, the rotational flow mixing channel 42B is of a cone structure, and the inclined plane of the cone and the bottom face form an included angle of 20-70 degrees. Through the nozzle structure, the three gases are mixed more fully, and the cracking and reforming effects of gaseous volatile matters are better.
In the solid-state bio-coke gasification unit 3, a gas-phase product rich in synthesis gas can be generated under the combined action of oxygen and water vapor; when the gaseous volatile matters generated in the microwave pyrolysis unit 2 are led into the pyrolysis reforming unit 4, multi-gas-path rotational flow mixing of the gaseous volatile matters, oxygen and water vapor is formed in the throat area, and primary reaction is carried out; the gas phase product rich in the synthesis gas generated by the solid bio-coke gasification unit 3 enters the throat area and carries out secondary reaction at high temperature, thus obtaining the synthesis gas product with higher quality.
The invention also provides a method for preparing synthesis gas by biomass thermal conversion, which comprises the following steps:
step S101, forming alternate feeding of the pretreated biomass raw materials with two different-size particles. The biomass feedstock may be a lignocellulose-containing material; the pretreatment specifically comprises airing, crushing and forming treatment.
Step S102, while heating the biomass raw material by microwaves, performing aerobic pyrolysis by oxygen flowing radially. Further, the oxygen flowing in the radial direction and the solid-phase biomass raw material moving downwards in the axial direction form cross flow for dedusting gas-phase products; aerobic pyrolysis supplies heat for microwave reaction, and the generated heat is transferred to the axle center through radial airflow; in addition, a large-particle low-temperature region and a small-particle high-temperature region are formed in the microwave field, the small-particle high-temperature region is pyrolyzed for generating oil gas, the oil gas flows to the large-particle low-temperature region with smaller air resistance, and heavy component tar in the oil gas is condensed and adhered to the large-particle low-temperature region in the flowing process. The microwave heating reaction time is 5-20 minutes, and the microwave power density is 0.1 multiplied by 10 5 ～1×10 5 W/m 3 Under the condition of (1), the temperature of the axial center area of the inner sleeve can reach 400-600 ℃ and the temperature of the circumferential area of the cylinder wall can reach 600-800 ℃ through the participation of aerobic pyrolysis; the temperature of the small particle high temperature area is 50-100 ℃ higher than that of the large particle low temperature area.
Aiming at the common problems of uneven internal and external heating, limited pyrolysis efficiency, low product quality control and the like of materials caused by gradually reducing microwave penetration depth due to temperature rise when high-capacity biomass is heated by microwaves, the limitation of the microwaves on the penetration depth of a raw material layer is utilized to initiate the decomposition of organic matters in external raw materials (namely biomass raw materials close to the circumference of a cylinder wall) and the generation of primary products, so that high-activity biomass rich in free radicals is formed; and the heterogeneous oxidation reaction of the oxidizing gas and the high-activity biomass rich in free radicals is fully utilized to supplement heat in the cavity, the high-temperature gas phase product generated in situ is used as a heat carrier, the driving gas flows up and down from the conventional shaft to be regulated into radial horizontal flow, namely, the gas flow flows from an external high-temperature region to an internal low-temperature region, so that the low-temperature region can be rapidly subjected to heat and mass transfer, the heavy components trapped in the low-temperature region are rapidly cracked to form light components and micromolecular gas, the release path of the pyrolysis gas phase product through the high-temperature region is weakened, the pyrolysis secondary reaction is reduced, in-situ filtration and dust removal of pyrolysis oil gas are realized, and the quality of the pyrolysis oil gas is improved.
Step S103, the generated gaseous volatile matters are led out from a gas phase channel which is arranged along the axis of the inner sleeve of the microwave pyrolysis unit.
Step S104, introducing solid bio-coke generated by microwave aerobic pyrolysis into a gasification unit, and generating a gas-phase product rich in synthesis gas under the combined action of oxygen and steam. Specifically, the solid bio-coke gasification unit is provided with a combustion zone and a reduction zone, wherein the temperature of the combustion zone is controlled to be 900-1200 ℃, and the temperature of the reduction zone is controlled to be 800-1000 ℃; the reaction time of the solid biological coke gasification section is 5-20 minutes.
Step S105, introducing the gaseous volatile matters generated in the step S103 into a cracking reforming unit, forming multi-gas-path rotational flow mixing of the gaseous volatile matters, oxygen and water vapor in a throat area, and performing primary reaction; the gas phase product rich in the synthesis gas generated in the step S104 enters the throat area and is subjected to secondary reaction at a high temperature state, so as to obtain the synthesis gas product. Wherein, the primary reaction conditions are as follows: oxygen flow rate is 0.5-5 m 3 And/h, the flow rate of the water vapor is 0.5-5 m 3 /h; the secondary reaction temperature is 1000-1200 ℃.
The synthesis gas product obtained through the steps S101 to S105 is rich in hydrogen and oxidationThe ratio of carbon, hydrogen and carbon monoxide is between 1.5 and 3.0; carbon dioxide content less than 25%, tar content less than 1mg/Nm 3 Ash content of not more than 10mg/Nm 3 The gas yield in the whole process is not lower than 2.5Nm 3 /kg of dry biomass.
Example 1
The following is presented in connection with fig. 1:
firstly, a feeding unit feeds biomass raw materials with two sizes into a microwave pyrolysis unit in an alternating continuous feeding mode, the height ratio of a small-size raw material bed layer to a large-size raw material bed layer is kept to be 1:0.2, and meanwhile, the microwave power density is 0.2 multiplied by 10 5 W/m 3 And oxygen flow rate 0.5m 3 Under the combined action of/h, the temperature of the cavity axis area of the microwave pyrolysis unit is 450 ℃, the temperature of the cylinder wall circumference area of the microwave pyrolysis unit is 650 ℃, the average temperature of the small-size raw material layer is higher than that of the large-size raw material layer by 60 ℃, and the pyrolysis reaction is carried out for 15 minutes under the conditions, so that high-quality gaseous volatile matters and byproduct solid biological coke are obtained.
Secondly, discharging the solid bio-coke from the bottom of the microwave pyrolysis unit and sending the solid bio-coke into the solid bio-coke gasification unit, wherein in the working gas 1 (the mixed gas of oxygen and nitrogen, the volume ratio of the oxygen to the nitrogen is 1:0.5, and the flow is controlled to be 1 m) 3 /h) and a working gas 2 (steam, flow rate controlled at 0.5m 3 Under the combined action of/h), the temperature of the combustion zone reaches 1000 ℃, the temperature of the reduction zone reaches 850 ℃, and the reaction is carried out for 15 minutes under the conditions to generate gaseous products rich in synthesis gas.
Then, the gaseous volatile matters released from the top of the microwave pyrolysis unit are introduced into the gaseous volatile matter decomposition reforming unit at an oxygen flow rate of 1.5m 3 /h and steam flow 3m 3 Carrying out primary reaction under the combined action of/h; and carrying out secondary reaction with gaseous products rich in synthesis gas from the solid bio-coke gasification unit, wherein the secondary reaction temperature is 1100 ℃, and obtaining high-quality synthesis gas products: wherein the ratio of hydrogen to carbon monoxide is 2.2, the content of carbon dioxide is 21.9%, the content of nitrogen is 9.2%, no tar exists in the gas, and the ash content is 10mg/Nm 3 The overall process gas yield was 3.8Nm 3 Kg of dry biomass。
The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. Any simple modifications, equivalent variations and modifications of the above-described exemplary embodiments should fall within the scope of the present invention.
Claims (18)
1. A system for producing synthesis gas by thermal conversion of biomass, comprising:
a feeding unit for providing biomass raw materials of two different-size particles and alternately feeding the biomass raw materials;
the cavity of the microwave pyrolysis unit is in an inner sleeve and an outer sleeve structure, and two biomass raw materials form moving bed layers which are alternately distributed along the axial direction in the inner sleeve; oxygen enters from the upper part of the space between the inner sleeve and the outer sleeve and flows along the radial direction at the middle lower part of the inner sleeve, the biomass raw material is heated by microwaves and is subjected to aerobic pyrolysis, and the generated gas-phase product flows out from a gas-phase channel extending along the axis of the inner sleeve.
2. The system for producing synthesis gas according to claim 1, wherein the feeding unit comprises:
the parallel double bins are respectively provided with biomass raw materials of the two particles with different sizes;
and the inlet end of the material conveying screw is respectively communicated with the double bins through Y-shaped pipelines, and the outlet end of the material conveying screw is communicated with the inner sleeve of the microwave pyrolysis unit.
3. The system for producing synthesis gas according to claim 1, wherein the microwave pyrolysis unit further comprises:
the microwave generators are arranged on the outer side of the cylinder wall of the outer sleeve and are uniformly distributed along the circumferential direction of the outer wall of the outer sleeve.
4. A system for preparing synthesis gas by thermal conversion of biomass as claimed in claim 3, wherein the wall surface of the middle lower part of the inner sleeve is provided with oxygen holes for oxygen to flow out radially; the middle and lower wall surfaces and the bottom of the gas phase channel are provided with gas phase product air holes.
5. The system for preparing synthesis gas by thermal conversion of biomass according to claim 4, wherein the height of the wall surface of the oxygen gas hole is 30% -60% of the whole height of the inner sleeve, and the aperture of the oxygen gas hole is 0.5-5 mm; the wall surface height of the gas phase product air hole is 1/3-2/3 of the whole height of the gas phase channel, the aperture of the gas phase product air hole is 0.2-2 mm, and the aperture ratio is 10-30%.
6. The system for producing synthesis gas according to claim 1, wherein the gas phase product produced by the microwave pyrolysis unit is a gaseous volatile component, the system further comprising:
the gaseous volatile component pyrolysis reforming unit is arranged at the upper part of the entrained flow bed and is provided with a throat structure, a nozzle which is circumferentially arranged along the entrained flow bed and radially extends is arranged in the throat area, and a multi-gas-path annular channel and a cyclone mixing channel are arranged in the nozzle and are used for introducing oxygen and water vapor and carrying out pyrolysis reforming on the gaseous volatile component.
7. The system for producing synthesis gas according to claim 6, wherein the multi-gas path annular channel comprises:
an inner ring channel which is arranged at the innermost side and is filled with oxygen;
a middle ring channel arranged outside the inner ring channel and communicated with the gaseous volatile component;
and the outer ring channel is arranged at the outer side of the middle ring channel and is filled with water vapor.
8. The system for preparing synthetic gas by thermal conversion of biomass according to claim 7, wherein the rotational flow mixing channel is of a cone structure, and the included angle between the inclined surface of the cone and the bottom surface is 20-70 °.
9. The system for producing synthesis gas according to claim 6, wherein the system further comprises:
the solid bio-coke gasification unit is arranged at the lower part of the entrained flow and receives solid bio-coke from the cavity of the microwave pyrolysis unit through a bio-coke conveying screw; the solid bio-coke gasification unit is provided with a combustion zone into which oxygen is introduced and a reduction zone into which water vapor is introduced; and the gasified product rises to enter the throat area for secondary reaction to obtain product gas.
10. The system for producing synthesis gas according to claim 9, wherein a grate is disposed between the combustion zone and the reduction zone; and a gas distributor which is obliquely arranged is arranged below the fire grate and at the corresponding position of the water vapor inlet.
11. A method for preparing synthesis gas by thermal conversion of biomass, which is characterized by comprising the following steps:
A. forming alternate feeding of the pretreated biomass raw materials with two different-size particles;
B. while microwave heating the biomass feedstock, performing aerobic pyrolysis with radially flowing oxygen;
C. and leading out the generated gaseous volatile matters from a gas phase channel which is arranged along the axis of the inner sleeve of the microwave pyrolysis unit.
12. The method for producing synthesis gas according to claim 11, wherein step B further comprises:
b1, forming cross flow with the radially flowing oxygen and the axially downward moving solid-phase biomass raw material for dedusting gas-phase products; aerobic pyrolysis supplies heat for microwave reaction, and the generated heat is transferred to the axle center through radial airflow;
b2, a large-particle low-temperature region and a small-particle high-temperature region are formed in the microwave field, the small-particle high-temperature region is pyrolyzed to generate oil gas, the oil gas flows to the large-particle low-temperature region with smaller air resistance, and heavy component tar in the oil gas is condensed and adhered to the large-particle low-temperature region in the flowing process.
13. The method for producing synthesis gas according to claim 11, wherein the biomass feedstock in step a is a lignocellulose-containing material; the pretreatment comprises airing, crushing and forming.
14. The method for preparing synthetic gas by thermal conversion of biomass according to claim 12, wherein the microwave heating reaction time is 5-20 minutes, and the microwave power density is 0.1 x 10 5 ～1×10 5 W/m 3 The method comprises the steps of carrying out a first treatment on the surface of the In the presence of aerobic pyrolysis, the temperature of the axis region of the inner sleeve reaches 400-600 ℃, and the temperature of the circumferential region of the cylinder wall reaches 600-800 ℃; the temperature of the small particle high temperature region is 50-100 ℃ higher than that of the large particle low temperature region.
15. The method for producing synthesis gas according to claim 11, wherein the method further comprises:
D. introducing solid bio-coke generated by microwave aerobic pyrolysis into a gasification unit, and generating a gas-phase product rich in synthesis gas under the combined action of oxygen and steam;
E. introducing the gaseous volatile matters generated in the step C into a cracking reforming unit, forming multi-gas-path rotational flow mixing of the gaseous volatile matters, oxygen and water vapor in a throat area, and performing primary reaction; and D, enabling the gas phase product rich in the synthesis gas generated in the step to enter the throat area and performing secondary reaction at a high temperature state to obtain the synthesis gas product.
16. The method for producing synthesis gas by thermal conversion of biomass according to claim 15, wherein the solid bio-char gasification unit has a combustion zone and a reduction zone, the combustion zone temperature is 900-1200 ℃, and the reduction zone temperature is 800-1000 ℃; the reaction time of the solid bio-coke gasification unit is 5-20 minutes.
17. The method for producing synthesis gas according to claim 15, wherein the primary reaction conditions in step E are: oxygen flow rate is 0.5-5 m 3 And/h, the flow rate of the water vapor is 0.5-5 m 3 /h; the secondary reaction temperature is 1000-1200 ℃.
18. The method for producing synthesis gas according to claim 15, wherein the synthesis gas product in step E is rich in hydrogen and carbon monoxide, and the ratio of hydrogen to carbon monoxide is between 1.5 and 3.0; carbon dioxide content less than 25%, tar content less than 1mg/Nm 3 Ash content of not more than 10mg/Nm 3 The gas yield in the whole process is not lower than 2.5Nm 3 /kg of dry biomass.
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