A method and system for producing syngas by biomass carbonization-gasification

Abstract

The present invention provides a method and a system for producing syngas by biomass carbonization - gasification. The method comprises the following steps: (1) treating a biomass raw material to obtain a first raw material; (2) mixing the first raw material and catalyst A evenly to obtain a second raw material; (3) introducing the second raw material into a carbonization reactor for reaction, and obtaining a solid-phase stream and a gas-phase stream after the reaction is completed; (4) mixing the solid-phase stream obtained in step (3) with catalyst B, and obtaining a third raw material after mixing evenly; (5) introducing the third raw material into a gasification reactor for activation, and further carrying out a steam gasification reaction in the presence of steam after the activation is completed to obtain a syngas product. The present invention converts biomass into a syngas product through the combined way of carbonization - gasification, and has the advantages of simple process, high syngas yield and high energy utilization rate.

Description

Technical Field

[0001] The present invention relates to the technical field of biomass utilization, and particularly relates to a method and a system for preparing syngas by biomass carbonization-gasification. Background Art

[0002] Due to the non-renewability of primary resources such as coal, petroleum and natural gas, as well as problems such as greenhouse effect and environmental protection in the use process, the clean and environment-friendly utilization of renewable biomass resources with both material and energy attributes shows great development potential and has become the focus of people's research and application. Biomass in the form of agricultural and forestry resources can generate syngas mainly composed of H2 and CO through gasification reaction after drying and pulverizing pretreatment, which is the main way to achieve the clean and environment-friendly utilization of biomass energy.

[0003] Syngas mainly composed of carbon monoxide and hydrogen is an important chemical "intermediate" and is the raw material for preparing Fischer-Tropsch synthetic oil. Using syngas as the raw material, methanol, synthetic ammonia, acrylic acid, gasoline, etc. can be prepared. The application and production of syngas are extremely important in the chemical industry. There have been many studies on the conversion of biomass syngas into high-value products such as chemical products. Patent CN102516004A uses biomass syngas with a low hydrogen-carbon ratio as the raw material and prepares light olefins through a two-step dimethyl ether method; Patent CN103468298A converts biomass syngas into liquid fuels with C5-C20 through Fischer-Tropsch reaction; CN104258913A prepares low-carbon mixed alcohols from biomass syngas.

[0004] The raw material range of syngas is very wide. It can be produced by gasifying solid fuels such as coal or coke, can also be prepared from light hydrocarbons such as natural gas and naphtha, and can also be produced by partial oxidation of heavy oil. However, coal, petroleum, natural gas, as well as coke oven gas, refinery gas, etc. contain a large amount of carbon, so carbon dioxide will be emitted during the production process, polluting the environment. Biomass resources have the characteristics of low sulfur content, wide resources, can be permanently utilized and do not increase the total amount of surface carbon dioxide circulation, and have received more and more extensive attention. Using biomass direct steam gasification to prepare syngas has very strict requirements for the gasifier. At the same time, the crude syngas produced has a high tar content and requires a very complex gas purification process. Patent CN110205162A discloses a method and device for producing biomass syngas. The biomass gasification temperature is as high as 900 °C, and the energy consumption is very high; compared with the biomass direct gasification technology, the tandem process of the biomass pyrolysis process and the coke gasification process can more precisely control the composition of the gas products according to the characteristics of the products. Patent CN109181781A discloses a method of co-gasifying seaweed and agricultural and forestry biomass in a pyrolysis-gasification mode and then using potassium, calcium, and sodium rich in seaweed coke as a biochar gasification catalyst. The temperature of seaweed in both the pyrolysis and coke gasification reaction sections is very high, and the purity of the syngas product is relatively low. Patent CN111378510A discloses a method and system for producing syngas using biomass, including processes such as biomass cracking, tar cracking, low-carbon hydrocarbon reforming, and biochar gasification. The process is lengthy, the energy consumption of the entire process is relatively high, and the syngas content in the product is relatively low. Patent CN107541292A discloses pyrolysis gasification with biomass as the raw material, and the gasification gas and oxygen carrier are used to prepare syngas to improve the gasification efficiency of biomass. However, there will be many new problems in the preparation and cyclic service life of the oxygen carrier and its coupling with the biomass gasification process, increasing the energy consumption and cost of the overall process.

[0005] The use prospect of biomass-based liquid fuels and chemicals ultimately depends on cost competitiveness, so reducing costs has become a key link in its economy. Therefore, the development of new biomass thermochemical conversion processes for syngas, inexpensive catalysts, and the reduction of process energy consumption have become the key points and difficulties in research. Summary of the Invention

[0006] To solve the technical problems existing in the prior art, the present invention provides a method and system for producing syngas by biomass carbonization-gasification, which converts biomass into syngas products through the combined method of carbonization-gasification, and has the advantages of simple process, high syngas yield, and high energy utilization rate.

[0007] In the first aspect of the present invention, a method for producing syngas by biomass carbonization-gasification in the first embodiment is provided, including the following steps:

[0008] (1) The biomass raw material is mixed with crude pyroligneous liquor, and after being uniformly mixed and dried, the first raw material is obtained;

[0009] (2) The first raw material and catalyst A are mixed, and after being uniformly mixed, the second raw material is obtained;

[0010] (3) The second raw material is introduced into a carbonization reactor for reaction, and after the reaction is completed, a solid-phase material flow and a gas-phase material flow are obtained;

[0011] (4) The solid-phase material flow obtained in step (3) is mixed with catalyst B, and after being uniformly mixed, the third raw material is obtained;

[0012] (5) The third raw material is introduced into a gasification reactor for activation, and after the activation is completed, a steam gasification reaction is further carried out in the presence of steam to obtain a syngas product.

[0013] In the second aspect of the present invention, a method for producing syngas by biomass carbonization-gasification according to the second embodiment is provided, including the following steps:

[0014] (1) The biomass raw material is mixed with crude pyroligneous liquor, and after being uniformly mixed and dried, the first raw material is obtained;

[0015] (2) The first raw material, activated carbon, and catalyst A are mixed, and after being uniformly mixed, the second raw material is obtained;

[0016] (3) The second raw material is introduced into a carbonization reactor for reaction, and after the reaction is completed, a solid-phase material flow and a gas-phase material flow are obtained;

[0017] (4) The solid-phase material flow obtained in step (3) is mixed with catalyst B, and after being uniformly mixed, the third raw material is obtained;

[0018] (5) The third raw material is introduced into a gasification reactor for activation, and after the activation is completed, a steam gasification reaction is further carried out in the presence of steam to obtain a syngas product.

[0019] Further, in the above method for producing syngas by biomass carbonization-gasification, the biomass raw material is any biomass containing lignocellulose such as forestry residues or agricultural residues, and more specifically, it can be one or several of straw, rice husk, wheat straw, wood blocks, leaves, and branches. The shape of the biomass raw material can be any shape such as sheet, round, cylindrical, conical, square, irregular shape, etc., and the maximum dimension of the raw material in the largest direction does not exceed 30 mm, preferably 1-25 mm.

[0020] Further, in the above method for producing syngas by biomass carbonization-gasification, the crude pyroligneous liquor includes wood vinegar and wood tar. Further, generally, the content of wood vinegar in the crude pyroligneous liquor is 60-70 wt%, which comes from the biomass pyrolysis or dry distillation process.

[0021] Further, in the above method for producing syngas by biomass carbonization-gasification, after the crude wood vinegar is obtained from the biomass pyrolysis or dry distillation system, it is directly used without any separation and purification process. The plant organic composite substances such as acids, alcohols, ketones, aldehydes, etc. in the crude wood vinegar contain a certain amount of organic functional groups. On the one hand, through the mixing process, the cellulose, hemicellulose and lignin in the biomass can absorb water and expand, achieving complete wetting of the aqueous substances, weakening the interaction force between different components of the biomass, and being more conducive to the carbonization process. On the other hand, through the mixing process, the wood tar in the crude wood vinegar can be evenly dispersed on the surface of the biomass raw material.

[0022] Further, in the above method for producing syngas by biomass carbonization-gasification, the weight ratio of the biomass raw material to the crude wood vinegar is 1:1 to 1:6, preferably 1:2 to 1:5.

[0023] Further, in the above method for producing syngas by biomass carbonization-gasification, the weight ratio of the biomass raw material to the activated carbon is 1:0.3 to 1:2, preferably 1:0.3 to 1:1.5.

[0024] Further, in the above method for producing syngas by biomass carbonization-gasification, the activated carbon is one or more of biomass-based activated carbon, pitch-based activated carbon, and petroleum coke-based activated carbon, preferably pitch-based activated carbon and / or petroleum coke-based activated carbon with a dense structure. Petroleum coke-based activated carbon refers to activated carbon with a rich pore structure obtained from petroleum coke through physical and / or chemical activation processes. Further preferably, the petroleum coke-based activated carbon is an activated carbon product obtained by activating the petroleum coke produced in the coking process, with a specific surface area of 1200 - 3000 m 2 / g, a pore diameter generally of 0.5 - 8 nm, and a mesopore ratio of 10% - 30%. For those skilled in the art, the physical and / or activation processes of the petroleum coke are well-known and can be selected from existing methods as needed.

[0025] Further, in the above method for producing syngas by biomass carbonization-gasification, during the biomass pyrolysis carbonization process, the rich pore structure and large pore volume of the activated carbon can achieve in-situ capture of the tar components pyrolyzed, especially the heavy tar components rich in polycyclic aromatic hydrocarbons. This not only reduces the tar content in the pyrolysis gas, but also provides sufficient space for the condensation reaction of the heavy tar components, depositing amorphous coke on the inner surface of the activated carbon, increasing the carbonization yield. At the same time, during the biochar gasification stage in the gasification reactor, it provides sufficient space for the amorphous biochar on the inner surface of the activated carbon to react with water vapor, improving the gasification reaction conversion rate of the biochar and the syngas yield.

[0026] Furthermore, in the above-mentioned method for producing synthesis gas by biomass carbonization-gasification, the activated carbon basically does not participate in the reaction during the biomass pyrolysis and carbonization process in the carbonization reactor, and a small amount of reaction will occur in the biochar gasification stage in the gasification reactor, but it has no effect on the properties of the synthesis gas product.

[0027] Furthermore, in the above-mentioned method for producing synthesis gas by biomass carbonization-gasification, the drying temperature in step (1) is 40-100°C, and vacuum drying is more preferably adopted.

[0028] Furthermore, in the above-mentioned method for producing synthesis gas by biomass carbonization-gasification, the weight ratio of the biomass raw material to the catalyst A is 60:1 to 10:1, preferably 50:1 to 10:1.

[0029] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization-gasification of biomass, catalyst A is a transition metal oxide, and the specific catalyst A is selected from one or more of nickel oxide, copper oxide, zinc oxide, ferroferric oxide, ferric oxide, cobalt oxide, vanadium pentoxide, manganese dioxide, and cerium dioxide, preferably one or more of nickel oxide, ferroferric oxide, ferric oxide, and cobalt oxide.

[0030] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization-gasification of biomass, the second raw material is preferably further crushed into powder, specifically, it can be crushed to a particle size of less than 10 mm and then enters the carbonization reactor for pyrolysis and carbonization reaction. The reaction temperature is 200-550°C, preferably 200-500°C; the reaction time is 0.2-2h, preferably 0.2-1h.

[0031] Furthermore, in the above-mentioned method for producing synthesis gas by biomass carbonization-gasification, the solid phase stream obtained by the carbonization reactor includes biochar, transition metal elements and transition metal oxides.

[0032] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization and gasification of biomass, the catalyst B is an alkali metal compound, more preferably a potassium compound and / or a sodium compound. The potassium compound can be specifically selected from one or more of potassium sulfate, potassium carbonate, potassium chloride, potassium nitrate, potassium tartrate, potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium iodide, potassium bromide, potassium hydroxide, and potassium fluoride; preferably one or more of potassium sulfate, potassium carbonate, potassium chloride, potassium nitrate, potassium tartrate, potassium iodide, potassium bromide, and potassium hydroxide. The sodium compound can be specifically selected from one or more of sodium sulfate, sodium carbonate, sodium bicarbonate, sodium chloride, sodium iodide, sodium bromide, and sodium hydroxide, preferably one or more of sodium carbonate, sodium bicarbonate, sodium bromide, and sodium hydroxide.

[0033] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization-gasification of biomass, the weight ratio of the catalyst B to the biomass raw material is 1:50 to 1:10, preferably 1:45 to 1:10.

[0034] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization and gasification of biomass, the catalyst B is mixed with the solid-phase stream from the carbonization reactor using a dry mixing method. Furthermore, before entering the gasification reactor, the solid-phase stream from the carbonization reactor is propelled and tumbled up and down with the catalyst B in a screw propeller to achieve uniform mixing, and the two are then used as feed to the gasification reactor.

[0035] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization-gasification of biomass, the solid phase material flow from the carbonization reactor and the catalyst B are mixed evenly and then added to the gasification reactor and first activated, and the activation temperature is 600-900°C, preferably 650-850°C; the activation is carried out under a reducing atmosphere or an inert atmosphere. Furthermore, the reducing atmosphere is any one or more of hydrogen, a hydrogen-helium mixture, a hydrogen-nitrogen mixture, and a hydrogen-water vapor mixture, and the volume proportion of hydrogen in the mixture can generally be 5% to 30%; the inert atmosphere is one of nitrogen and helium.

[0036] Furthermore, in the above-mentioned method for producing synthesis gas by biomass carbonization-gasification, the reactions occurring in the carbonization reactor are mainly biomass carbonization reaction and biomass pyrolysis reaction, and the transition metal oxide (catalyst A) has a significant catalytic effect on the pyrolysis and carbonization reactions of biomass. At the same time, it can also react with the reducing substances such as carbon and hydrogen generated by the reaction products to in situ generate active transition metal elements that are highly dispersed on the surface of biochar, and the solid phase material flow at the outlet of the carbonization reactor contains transition metal oxides and transition metal elements in different proportions.

[0037] Furthermore, in the above-mentioned method for producing synthesis gas by carbonization-gasification of biomass, in the gasification reactor, the solid-phase material flow from the carbonization reactor containing transition metal oxides and transition metal elements is evenly mixed with catalyst B, and then an activation reaction is first carried out at a higher reaction temperature in a reducing atmosphere or an inert atmosphere. A strong interaction occurs between the alkali metal compound (catalyst B) and the transition metal oxide, forming an intermediate substance that can improve the reaction activity of the alkali metal compound and fix the alkali metal at the same time. This can significantly improve the water vapor gasification reaction activity and reduce the gasification reaction temperature. At the same time, it also plays a good role in fixing the alkali metal element, greatly reducing the volatilization amount of the alkali metal element.

[0038] Further, in the above method for producing syngas by biomass carbonization - gasification, the gasification reaction temperature in the gasification reactor is 700 - 950 °C, preferably 750 - 900 °C; the gasification reaction time is 20 - 90 min, preferably 20 - 75 min.

[0039] Further, in the above method for producing syngas by biomass carbonization - gasification, the weight ratio of steam to bio - char is 0.1 - 10, preferably 0.2 - 8.

[0040] Further, in the above method for producing syngas by biomass carbonization - gasification, the gaseous feed stream from the carbonization reactor is volatile gas, mainly including combustible gases, volatile tar components, etc. that escape from the carbonization reactor in gaseous form during biomass pyrolysis and carbonization.

[0041] Further, in the above method for producing syngas by biomass carbonization - gasification, the gaseous feed stream from the carbonization reactor can enter a burner for full combustion (the full combustion generally means that the combustion products are only carbon dioxide and water), and the heat generated by the gas combustion can be supplied to the steam generator, carbonization reactor, and gasification reactor for use. Preferably, it is first supplied to the steam generator for use, and the excess heat is used to assist the carbonization reactor and gasification reactor.

[0042] The third aspect of the present invention provides a system for producing syngas by biomass carbonization - gasification, including the following:

[0043] A first mixer for receiving and mixing biomass raw materials and crude wood vinegar liquid;

[0044] A first dryer for receiving and drying the mixed material from the first mixer, and obtaining the first raw material after drying;

[0045] A second mixer for receiving the first raw material from the first dryer, catalyst A, and optionally activated carbon, and uniformly mixing them to obtain the second raw material;

[0046] A carbonization reactor for receiving the second raw material from the second mixer, and obtaining a solid - phase feed stream and a gaseous feed stream after the reaction;

[0047] A gasification reactor for receiving the solid - phase feed stream from the carbonization reactor and catalyst B, and further carrying out steam gasification reaction in the presence of steam after activation of the solid - phase feed stream and catalyst B to obtain syngas products.

[0048] Further, in the above system for producing syngas by biomass carbonization - gasification, the first mixer and the second mixer can adopt any one of the existing high - speed rotary pulverizers, ball mills, solid - phase pulverizing homogenizers, etc. in the art.

[0049] Further, in the above system for producing syngas by biomass carbonization - gasification, the first dryer can be any one of the existing devices in the art that can achieve the drying function, specifically, it can be any one or several of a blast drying oven, a vacuum drying oven, a hot air circulation oven, etc.

[0050] Further, in the above system for producing syngas by biomass carbonization - gasification, the carbonization reactor can be any one of the existing carbonization reactors in the art. Specifically, it can be any one of a biomass microwave vertical fixed - bed reactor, a biomass screw - propelled carbonization reactor, a biomass rotary furnace carbonization reactor, etc.

[0051] Further, in the above system for producing syngas by biomass carbonization - gasification, the solid - phase material flow from the carbonization reactor is uniformly mixed with catalyst B in a screw propeller by means of propulsion, up - and - down turning, etc. before entering the gasification reactor, and they are jointly used as the feed of the gasification reactor.

[0052] Further, in the above system for producing syngas by biomass carbonization - gasification, the gasification reactor can be any one of a microwave vertical fixed - bed gasification reactor, a microwave fluidized - bed gasification reactor, an electrically heated vertical fixed - bed reactor, etc.

[0053] Further, in the above system for producing syngas by biomass carbonization - gasification, it includes a steam generator, which is used to generate steam.

[0054] Further, in the above system for producing syngas by biomass carbonization - gasification, it includes a burner. The gas - phase material flow from the carbonization reactor enters the burner for full combustion (the full combustion generally means that the combustion products are only carbon dioxide and water). The heat generated by the gas combustion can be supplied to the steam generator, the carbonization reactor and the gasification reactor for use. Preferably, it is first supplied to the steam generator for use, and the excess heat is used to assist the carbonization reactor and the gasification reactor.

[0055] Compared with the prior art, the beneficial technical effects of the method and system for producing syngas by biomass carbonization - gasification of the present invention are as follows:

[0056] (1) The method of the present invention converts biomass raw materials into syngas products through the combination of carbonization - gasification, which has the advantages of simple process, high syngas yield, and high energy utilization rate. At the same time, it broadens the application scope of biomass.

[0057] (2) The method of the present invention returns the crude wood vinegar obtained from biomass pyrolysis or dry distillation to the method of the present invention, and uses the crude wood vinegar to pre - treat the biomass raw materials. This not only finds a suitable utilization way for the low - value - added crude wood vinegar, but also can effectively promote the biomass carbonization process, and at the same time does not affect the product properties.

[0058] (3) In the method of the present invention, during the biomass carbonization process, by adding petroleum coke-based activated carbon, in-situ capture of tar components is achieved, the coke yield is increased. At the same time, in the biochar gasification stage, sufficient space is provided for the amorphous biochar on the inner surface of the activated carbon to react with water vapor, maximizing the gasification reaction conversion rate and syngas yield of the biochar.

[0059] (4) The catalyst raw materials used in the method of the present invention have a wide range of sources, can be obtained from natural ores and seawater, and are inexpensive, greatly reducing the catalytic cost of biochar steam gasification. They can be recycled by the water-soluble method or without recycling. In the biochar gasification process, two low-cost catalysts, transition metal oxides and potassium salts, are used. The transition metal oxides not only play a catalytic role in the carbonization reaction of biomass, but their reaction products can further effectively couple with alkali metal salts and have a strong interaction during the catalyst activation process, forming an intermediate substance that can improve the reaction activity of alkali metal salts and fix alkali metals, significantly improving the steam gasification reaction activity, reducing the gasification reaction temperature. At the same time, it also plays a good role in the fixation of alkali metals, greatly reducing the volatilization amount of alkali metals.

[0060] (5) In the method of the present invention, the gaseous feed stream generated in the carbonization reactor is sent to the burner for combustion at a high temperature. The tar components are burned together with combustible gases in a gaseous state, avoiding environmental pollution caused by tar emissions and gas purification, preventing pipeline blockage caused by tar condensation, and solving the oil-gas separation problem, greatly simplifying the reaction steps. At the same time, by using a regenerative heat exchanger, the huge heat generated by combustion is supplied to the steam generator, carbonization reactor, and gasification reactor for use, providing heat for the reaction and assisting the energy supply of the entire process, ensuring the stable operation of the reaction. Description of the Drawings

[0061] Figure 1 It is a schematic flow diagram of the method for producing syngas by biomass carbonization-gasification of the present invention. Detailed Embodiments

[0062] The present invention will be described in detail below in conjunction with embodiments, but the protection scope of the present invention is not limited by the embodiments.

[0063] Unless otherwise clearly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "having" etc. will be understood to include the stated elements or components, without excluding other elements or other components.

[0064] In this article, for the convenience of description, spatial relative terms such as "below", "beneath", "under", "above", "over", "on" etc. may be used to describe the relationship between one element or feature and another element or feature in the drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation in addition to the orientation depicted in the figures. For example, if an object in the figure is flipped, an element described as "below" or "under" another element or feature will be oriented "above" that element or feature. Thus, the exemplary term "below" can encompass both the below and above directions. The object can also have other orientations (rotated 90 degrees or other orientations) and the spatial relative terms used herein should be interpreted accordingly.

[0065] In this article, terms such as "first", "second" etc. are used to distinguish two different elements or parts, and are not used to define a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second" etc. can also be interchanged with each other.

[0066] In this article, all numerical values of parameters (e.g., quantity or condition) should be understood to be modified by the term "about" in all cases, whether or not "about" actually appears before the numerical value.

[0067] In this article, the specific surface area and pore size distribution curve of the sample are obtained from the nitrogen adsorption - desorption curve on a Micromeritics ASAP 2020 type adsorption instrument. The operating temperature is -196 °C (liquid nitrogen temperature). The sample is pre - dehydrated at 300 °C under nitrogen protection before testing. The specific surface area and pore size distribution are calculated by the BET method and DFT method respectively.

[0068] Example 1

[0069] Weigh 100 g of petroleum coke (from the coking unit of Jinling Branch), mix the petroleum coke evenly with 280 g of potassium hydroxide, activate it at 800 °C for 40 min in a nitrogen atmosphere, cool it to room temperature, wash the product with dilute hydrochloric acid (concentration 2 wt%) and deionized water in sequence until neutral, and dry it at 105 °C for 10 h in a forced - air drying oven to obtain petroleum - coke - based activated carbon. The specific surface area measured by a physical adsorption instrument is 1896 m 2 / g, the mesopore ratio is 18%, and the pore size is 0.5 - 8 nm.

[0070] Example 2

[0071] Weigh 30.6 g of Picea koraiensis, add 30.6 g of crude wood vinegar (from the pyrolysis process of mixed miscellaneous woods, reddish - brown, density 1.0041 g / cm 3, with a pH of 4.08, mainly composed of water. In the organic component, phenols account for 11.36%, organic acids for 21.96%, ketones for 18.79%, and furan derivatives for 8.88%. The rest are alcohols, lipids, aldehydes, etc. This crude wood vinegar liquid was used in all other examples.), stirred and mixed evenly, left to soak for 6 h, dried in vacuum at 60 °C for 8 h to obtain the first raw material. Then, the first raw material, 9.18 g of the petroleum coke-based activated carbon obtained in Example 1, and 0.72 g of iron(III) oxide were mixed, and then further pulverized in a pulverizer to less than 10 mm to obtain the second raw material.

[0072] The second raw material was added to a carbonization reactor for reaction. The reaction temperature was 350 °C. The solid-phase material flow generated by the reaction was mixed evenly with 1.38 g of potassium sulfate in a screw feeder, and then activated at 600 °C under a nitrogen-hydrogen mixed atmosphere (hydrogen volume fraction of 20%) for 50 min; further steam was introduced for gasification. The gasification reaction conditions were: gasification temperature 800 °C, atmospheric pressure, steam flux 0.3 mL / min, and gasification time 60 min. The volume fraction of syngas in the gas at the outlet of the gasification reactor was 96.1%, and the syngas yield of the entire process was 576 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor were sent to a burner for combustion at a high temperature. Through a regenerative heat exchanger, the huge heat generated by the combustion of the volatile components was supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the entire process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating was required to ensure the stable operation of the reaction.

[0073] Example 3

[0074] Weigh 35.2 g of Picea koraiensis, add 211.2 g of crude wood vinegar liquid, stir and mix evenly, leave to soak for 6 h, dry in vacuum at 80 °C for 20 h to obtain the first raw material. Mix the first raw material 1, 70.4 g of the petroleum coke-based activated carbon obtained in Example 1, and 0.54 g of iron(III) oxide, and then further pulverize in a pulverizer to less than 10 mm to obtain the second raw material.

[0075] The second raw material is added to the carbonization reactor for reaction. The reaction temperature is 500 °C. The solid-phase material flow generated by the reaction is mixed evenly with 1.18 g of potassium chloride in a screw feeder and then enters the gasification reactor. First, it is activated at 600 °C for 40 min in a nitrogen-hydrogen mixed atmosphere (the volume fraction of hydrogen is 15%); then, steam is introduced for steam gasification reaction. The reaction conditions are: gasification temperature 800 °C, atmospheric pressure, steam flux 0.3 mL / min. The proportion of syngas in the gas at the outlet of the gasification reactor is 94.7%, and the syngas yield of the whole process is 672 g of syngas / kg of biomass. Meanwhile, the volatile components generated in the carbonization reactor are sent to the burner for combustion at a high temperature. Through the regenerative heat exchanger, the heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is needed to ensure the stable operation of the reaction.

[0076] Example 4

[0077] Weigh 39.4 g of willow wood, add 120.4 g of crude wood vinegar liquid, stir and mix evenly, let it stand for impregnation for 6 h, and dry it at 80 °C under vacuum for 8 h to obtain the first raw material. Mix the first raw material, 39.4 g of the petroleum coke-based activated carbon obtained in Example 1, and 0.49 g of vanadium pentoxide, and then further pulverize it in a pulverizer to less than 10 mm to obtain the second raw material.

[0078] The second raw material is added to the carbonization reactor for reaction. The reaction temperature is 550 °C. The solid-phase material flow generated by the reaction is mixed evenly with 2.41 g of potassium bromide in a screw feeder and then activated at 650 °C for 45 min in a nitrogen-hydrogen mixed atmosphere (the volume fraction of hydrogen is 15%); steam is introduced for gasification. The reaction conditions are: gasification temperature 850 °C, atmospheric pressure, steam flux 0.45 mL / min, reaction time 40 min. The proportion of syngas in the gas at the outlet of the gasification reactor is 93.7%, and the syngas yield of the whole process is 608 g of syngas / kg of biomass. Meanwhile, the volatile components generated in the carbonization reactor are sent to the burner for combustion at a high temperature. Through the regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is needed to ensure the stable operation of the reaction.

[0079] Example 5

[0080] Weigh 40.3 g of hazelwood, add 80.6 g of crude wood vinegar, stir and mix evenly, let it stand for impregnation for 6 h, and dry it in vacuum at 80 °C for 8 h to obtain the first raw material. Mix the first raw material with 24.2 g of the petroleum coke-based activated carbon obtained in Example 1 and 0.88 g of iron tetroxide, and then further pulverize it in a pulverizer to less than 10 mm to obtain the second raw material.

[0081] Add the second raw material into a biomass carbonization reactor for reaction. The reaction temperature is 300 °C. The solid-phase material flow generated by the reaction is mixed evenly with 2.13 g of potassium tartrate in a screw feeder, and activation is carried out at 550 °C under a helium-hydrogen mixed atmosphere (the volume fraction of hydrogen is 30%) for 45 min; water vapor is introduced for gasification reaction. The reaction conditions are: gasification temperature 950 °C, atmospheric pressure, the water vapor flux is 0.55 mL / min, and the proportion of syngas in the gas at the outlet of the gasification reactor is 96.7%. The syngas yield of the whole process is 591 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to a burner for combustion at a high temperature state. Through a regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is required to ensure the stable operation of the reaction.

[0082] Example 6

[0083] Weigh 40.1 g of Pinus sylvestris var. mongolica branches and twigs, add 98.2 g of crude wood vinegar, stir and mix evenly, let it stand for impregnation for 6 h, and dry it in vacuum at 70 °C for 8 h to obtain the first raw material. Mix the first raw material with 28.1 g of the petroleum coke-based activated carbon obtained in Example 1 and 0.61 g of cobalt oxide, and then further pulverize it in a pulverizer to less than 10 mm to obtain the second raw material.

[0084] The second raw material is added to the carbonization reactor for reaction. The reaction temperature is 400 °C. The solid-phase material flow generated by the reaction is mixed evenly with 1.45 g of potassium nitrate in a spiral feeder and then enters the gasification reactor. It is activated at 400 °C under a nitrogen-hydrogen mixed atmosphere (hydrogen volume fraction is 5%) for 25 min. Steam is introduced for gasification reaction. The reaction conditions are: gasification temperature 900 °C, atmospheric pressure, steam flux 0.5 mL / min. The proportion of syngas in the gas at the outlet of the gasification reactor is 95.6%. The syngas yield of the whole process is 649 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to the burner for combustion at a high temperature. Through the regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is needed to ensure the stable operation of the reaction.

[0085] Example 7

[0086] Weigh 30.6 g of Picea koraiensis, add 30.6 g of crude wood vinegar liquid, stir and mix evenly, let it stand for impregnation for 6 h, and dry it at 60 °C under vacuum for 8 h to obtain the first raw material. Then mix the first raw material with 0.72 g of iron oxide, and further pulverize it in a pulverizer to less than 10 mm to obtain the second raw material.

[0087] The second raw material is added to the carbonization reactor for reaction. The reaction temperature is 350 °C. The solid-phase material flow generated by the reaction is mixed evenly with 1.38 g of potassium sulfate in a spiral feeder, and then activated at 600 °C under a nitrogen-hydrogen mixed atmosphere (hydrogen volume fraction is 20%) for 50 min. Further steam is introduced for gasification. The gasification reaction conditions are: gasification temperature 800 °C, atmospheric pressure, steam flux 0.3 mL / min, gasification time 60 min. The proportion of syngas in the gas at the outlet of the gasification reactor is 86.7%. The syngas yield of the whole process is 497 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to the burner for combustion at a high temperature. Through the regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is needed to ensure the stable operation of the reaction.

[0088] Comparative Example 1

[0089] Compared with Example 2, the difference is that crude wood vinegar liquid is not used and the biomass raw material is not pretreated.

[0090] Weigh 30.6 g of Picea koraiensis, 9.18 g of the petroleum coke-based activated carbon obtained in Example 1, and 0.72 g of ferric oxide, mix them, and then further pulverize them in a pulverizer to less than 10 mm to obtain the second raw material.

[0091] Add the second raw material to a carbonization reactor for reaction. The reaction temperature is 350 °C. The solid-phase material flow generated by the reaction is mixed evenly with 1.38 g of potassium sulfate in a screw feeder, and then activated at 600 °C under a nitrogen-hydrogen mixed atmosphere (hydrogen volume fraction is 20%) for 50 min. Further, steam is introduced for gasification. The gasification reaction conditions are: gasification temperature 800 °C, normal pressure, steam flux 0.3 mL / min, and gasification time 60 min. The volume fraction of syngas in the gas at the outlet of the gasification reactor is 87.3%, and the syngas yield of the whole process is 465 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to a burner for combustion at a high temperature. Through a regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is required to ensure the stable operation of the reaction.

[0092] Comparative Example 2

[0093] Compared with Example 2, the difference is that the physical properties of the added activated carbon do not meet the requirements.

[0094] Weigh 30.6 g of Picea koraiensis, add 30.6 g of crude wood vinegar, stir and mix evenly, let it stand for impregnation for 6 h, and dry it at 60 °C under vacuum for 8 h to obtain the first raw material. Then mix the first raw material, 9.18 g of the petroleum coke-based activated carbon obtained in Example 1 (specific surface area 1003 m 2 / g, mesopore rate 4%, pore size mainly micropores below 1 nm), and 0.72 g of ferric oxide, and then further pulverize them in a pulverizer to less than 10 mm to obtain the second raw material.

[0095] The second raw material is added to the carbonization reactor for reaction. The reaction temperature is 350 °C. The solid-phase material flow generated by the reaction is mixed evenly with 1.38 g of potassium sulfate in a screw feeder, and then activated at 600 °C under a nitrogen-hydrogen mixed atmosphere (the volume fraction of hydrogen is 20%) for 50 min. Further, steam is introduced for gasification. The gasification reaction conditions are: gasification temperature 800 °C, normal pressure, steam flux 0.3 mL / min, gasification time 60 min. The proportion of syngas in the gas at the outlet of the gasification reactor is 88.3%, and the syngas yield of the whole process is 508 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to the burner for combustion at a high temperature. Through the regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is needed to ensure the stable operation of the reaction.

[0096] Comparative Example 3

[0097] Compared with Example 3, the difference is that catalyst A is not used.

[0098] Weigh 35.2 g of Picea koraiensis, add 211.2 g of crude wood vinegar, stir and mix evenly, let it stand for impregnation for 6 h, and dry it at 80 °C under vacuum for 20 h to obtain the first raw material. Mix 1 part of the first raw material with 70.4 g of the petroleum coke-based activated carbon obtained in Example 1, and then further grind it into powder with a particle size of less than 10 mm in a pulverizer to obtain the second raw material.

[0099] The second raw material is added to the carbonization reactor for reaction. The reaction temperature is 500 °C. The solid-phase material flow generated by the reaction is mixed evenly with 1.18 g of potassium chloride in a screw feeder, enters the gasification reactor, and steam is introduced for steam gasification reaction. The reaction conditions are: gasification temperature 800 °C, normal pressure, steam flux 0.3 mL / min. The proportion of syngas in the gas at the outlet of the gasification reactor is 94.7%, and the syngas yield of the whole process is 213 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to the burner for combustion at a high temperature. Through the regenerative heat exchanger, the heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is needed to ensure the stable operation of the reaction.

[0100] Comparative Example 4

[0101] Compared with Example 4, the difference is that catalyst B is not used.

[0102] Weigh 39.4 g of willow wood, add 120.4 g of crude wood vinegar, stir and mix evenly, let it stand for impregnation for 6 h, and dry it at 80 °C under vacuum for 8 h to obtain the first raw material. Mix the first raw material, 39.4 g of the petroleum coke-based activated carbon obtained in Example 1, and 0.49 g of vanadium pentoxide, and then further pulverize it in a pulverizer to less than 10 mm to obtain the second raw material.

[0103] Add the second raw material into a carbonization reactor for reaction. The reaction temperature is 550 °C. The solid-phase material flow generated by the reaction is activated at 650 °C under a nitrogen-hydrogen mixed atmosphere (the volume fraction of hydrogen is 15%), and the activation time is 45 min; steam is introduced for gasification. The reaction conditions are: gasification temperature 850 °C, atmospheric pressure, steam flux 0.45 mL / min, reaction time 40 min. The proportion of syngas in the gas at the outlet of the gasification reactor is 78.1%, and the syngas yield of the whole process is 161 g of syngas / kg of biomass. At the same time, the volatile components generated in the carbonization reactor are sent to the burner for combustion in a high-temperature state. Through the regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing guarantee for the energy supply of the whole process, greatly reducing the energy consumption of the process itself, and only a small amount of auxiliary heating is required to ensure the stable operation of the reaction.

[0104] Through the analysis of the data of Examples 2-7 and Comparative Examples 1-4, it can be seen that in the biomass carbonization process of the method of the present invention, the maximum yield of biochar is achieved by the combined use of methods such as impregnation with crude wood vinegar, addition of petroleum coke-based activated carbon, and temperature adjustment. The transition metal oxide not only plays a catalytic role in the carbonization reaction of biomass, but at the same time its reaction product is effectively coupled with the alkali metal salt. During the activation process of the catalyst, a strong interaction occurs, forming an intermediate substance that can improve the reaction activity of the alkali metal salt and fix the alkali metal, which can significantly improve the steam gasification reaction activity, reduce the gasification reaction temperature, and at the same time, it also plays a good role in the fixation of alkali metals, greatly reducing the volatilization amount of alkali metals.

[0105] In the method of the present invention, the volatile components generated in the carbonization reactor are sent to the burner for combustion in a high-temperature state. The tar components burn together with the combustible gas in a gaseous state, avoiding environmental pollution caused by tar emissions and gas purification, preventing pipeline blockage caused by tar condensation, and more importantly, avoiding the complex problem of oil-gas separation, greatly simplifying the reaction steps. Through the regenerative heat exchanger, the huge heat generated by the combustion of the volatile components is supplied to the steam generator, the carbonization reactor, and the gasification reactor, providing heat and reaction temperature for the reaction, providing most of the energy supply for the whole process, ensuring the stable operation of the reaction, and greatly reducing the energy consumption of the reaction.

[0106] The foregoing description of the specific exemplary embodiments of the present invention is for purposes of illustration and exemplification. These descriptions are not intended to limit the invention to the precise forms disclosed, and it is apparent that many changes and variations are possible in light of the above teachings. The purpose of selecting and describing the exemplary embodiments is to explain the specific principles of the invention and its practical applications, so that those skilled in the art can implement and utilize the various different exemplary embodiments of the invention, as well as various different selections and changes. Any simple modifications, equivalent variations, and embellishments made to the above exemplary embodiments shall fall within the protection scope of the present invention.

Claims

1. A method for producing synthesis gas by carbonization-gasification of biomass, comprising the following steps: (1) A biomass raw material and crude wood vinegar are mixed, mixed evenly and dried to obtain a first raw material; the biomass raw material is any biomass containing lignocellulose; the crude wood vinegar is obtained from a biomass pyrolysis process and includes wood vinegar and wood tar; (2) mixing the first raw material and catalyst A, and mixing them evenly to obtain a second raw material, wherein catalyst A is a transition metal oxide; (3) introducing the second raw material into a carbonization reactor for reaction, and obtaining a solid phase stream and a gas phase stream after the reaction is completed; (4) mixing the solid phase stream obtained in step (3) with catalyst B, and mixing them evenly to obtain a third raw material, wherein the catalyst B is an alkali metal compound; (5) The third raw material is introduced into a gasification reactor for activation. After activation, it is further subjected to steam gasification reaction in the presence of water vapor to obtain a synthesis gas product.

2. A method for producing synthesis gas by carbonization-gasification of biomass, comprising the following steps: (1) A biomass raw material and crude wood vinegar are mixed, mixed evenly and dried to obtain a first raw material; the biomass raw material is any biomass containing lignocellulose; the crude wood vinegar is obtained from a biomass pyrolysis process and includes wood vinegar and wood tar; (2) mixing the first raw material, activated carbon, and catalyst A, and mixing them evenly to obtain a second raw material, wherein catalyst A is a transition metal oxide; (3) introducing the second raw material into a carbonization reactor for reaction, and obtaining a solid phase stream and a gas phase stream after the reaction is completed; (4) mixing the solid phase stream obtained in step (3) with catalyst B, and mixing them evenly to obtain a third raw material, wherein the catalyst B is an alkali metal compound; (5) The third raw material is introduced into a gasification reactor for activation. After activation, it is further subjected to steam gasification reaction in the presence of water vapor to obtain a synthesis gas product.

3. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The content of wood vinegar in the crude wood vinegar is 60-70wt%.

4. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of the biomass raw material to the crude wood vinegar is 1:1 to 1:

6.

5. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of the biomass raw material to the crude wood vinegar is 1:2 to 1:

5.

6. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 2, wherein: The weight ratio of biomass raw material to activated carbon is 1:0.3 to 1:

2.

7. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 2, wherein: The weight ratio of biomass raw material to activated carbon is 1:0.3 to 1:1.

5.

8. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 2, wherein: The activated carbon is one or more of biomass-based activated carbon, asphalt-based activated carbon, and petroleum coke-based activated carbon.

9. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 8, wherein: Petroleum coke-based activated carbon is an activated carbon product obtained by activating petroleum coke produced in the coking process. Its specific surface area is 1200~3000m 2 / g, the pore size is 0.5~8nm, and the mesoporosity is 10%~30%.

10. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The drying temperature in step (1) is 40-100°C.

11. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The drying in step (1) is carried out by vacuum drying.

12. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of the biomass raw material to the catalyst A is 60:1 to 10:

1.

13. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of the biomass raw material to the catalyst A is 50:1 to 10:

1.

14. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: Catalyst A is one or more of nickel oxide, copper oxide, zinc oxide, ferroferric oxide, ferrous oxide, cobalt oxide, vanadium pentoxide, manganese dioxide, and cerium dioxide.

15. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: Catalyst A is one or more of nickel oxide, ferrosoferric oxide, ferric oxide, and cobalt oxide.

16. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The second raw material is crushed into powder and then enters the carbonization reactor for pyrolysis and carbonization reaction. The reaction temperature is 200-550° C. and the reaction time is 0.2-2 hours.

17. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The second raw material is crushed into powder and then enters the carbonization reactor for pyrolysis and carbonization reaction. The reaction temperature is 200-500° C. and the reaction time is 0.2-1 hour.

18. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: Catalyst B is a potassium-containing compound and / or a sodium-containing compound, the potassium-containing compound is selected from one or more of potassium sulfate, potassium carbonate, potassium chloride, potassium nitrate, potassium tartrate, potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium iodide, potassium bromide, potassium hydroxide, and potassium fluoride; the sodium-containing compound is selected from one or more of sodium sulfate, sodium carbonate, sodium bicarbonate, sodium chloride, sodium iodide, sodium bromide, and sodium hydroxide.

19. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: Catalyst B is a potassium-containing compound and / or a sodium-containing compound, wherein the potassium-containing compound is selected from one or more of potassium sulfate, potassium carbonate, potassium chloride, potassium nitrate, potassium tartrate, potassium iodide, potassium bromide, and potassium hydroxide; and the sodium-containing compound is selected from one or more of sodium carbonate, sodium bicarbonate, sodium bromide, and sodium hydroxide.

20. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of catalyst B to biomass raw material is 1:50 to 1:

10.

21. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of catalyst B to biomass raw material is 1:45 to 1:

10.

22. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The solid phase material flow from the carbonization reactor and the catalyst B are evenly mixed and added to the gasification reactor and first activated at a temperature of 600 to 900°C. The activation is carried out under a reducing atmosphere or an inert atmosphere. The reducing atmosphere is any one or more of hydrogen, a hydrogen-helium mixture, a hydrogen-nitrogen mixture, and a hydrogen-water vapor mixture, with the volume proportion of hydrogen in the mixture being 5% to 30%. The inert atmosphere is one of nitrogen and helium.

23. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 22, wherein: The activation temperature is 650-850℃.

24. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The gasification reaction temperature in the gasification reactor is 700-950° C., and the gasification reaction time is 20-90 minutes.

25. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The gasification reaction temperature in the gasification reactor is 750-900° C., and the gasification reaction time is 20-75 minutes.

26. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of water vapor to biochar is 0.1 to 10.

27. The method for producing synthesis gas by carbonization and gasification of biomass according to claim 1 or 2, wherein: The weight ratio of water vapor to biochar is 0.2 to 8.

28. A system for producing synthesis gas by carbonization and gasification of biomass for implementing the method for producing synthesis gas by carbonization and gasification of biomass as claimed in any one of claims 1 to 27, comprising the following contents: a first mixer for receiving and mixing the biomass raw material and the crude wood vinegar; a first dryer for receiving and drying the mixed material from the first mixer to obtain a first raw material after drying; a second mixer for receiving the first raw material and catalyst A from the first dryer and mixing them uniformly to obtain the second raw material; or for receiving the first raw material, catalyst A, and activated carbon from the first dryer and mixing them uniformly to obtain the second raw material; A carbonization reactor is used to receive the second raw material from the second mixer and obtain a solid phase material flow and a gas phase material flow after the reaction is completed; The gasification reactor is used to receive the solid phase material flow and catalyst B from the carbonization reactor. After activation, the solid phase material flow and catalyst B are further subjected to steam gasification reaction in the presence of water vapor to obtain a synthesis gas product.

29. The system for producing synthesis gas by carbonization and gasification of biomass according to claim 28, wherein: A water vapor generator is included for generating water vapor.

30. The system for producing synthesis gas by carbonization and gasification of biomass according to claim 28, wherein: Including burner.

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