System and method for preparing green methanol from biomass

Abstract

The invention discloses a system and a method for preparing green methanol from biomass, relates to the technical field of methanol preparation, and solves the problems of high cost and low efficiency during preparation of green methanol. Meanwhile, the problem that the distillation effect is poor when green methanol is prepared is solved. The system for preparing green methanol from biomass comprises a biomass liquefaction unit and a green methanol unit, the green methanol unit comprises a methanol rectifying tower, a gas-liquid flow guide assembly is arranged at the center of the interior of the methanol rectifying tower, and automatic gas-liquid distillation mechanisms are arranged on the upper side and the lower side of the gas-liquid flow guide assembly. According to the method, a distributed biomass liquefaction and centralized green methanol synthesis technical route is adopted, the problems and cost of biomass collection, storage and transportation are solved, the chemical land demand is reduced, and meanwhile, the large-scale effect of a green methanol factory is embodied. Meanwhile, during methanol distillation, gas rising and liquid falling are carried out respectively, and the methanol distillation effect is better.

Description

Technical Field

[0001] The present invention relates to the technical field of methanol preparation, and in particular to a system and method for preparing green methanol from biomass. Background Art

[0002] Against the backdrop of global climate change and low-carbon energy transformation, green methanol is widely considered to be one of the most important renewable clean fuels and raw materials in the future, and is of great significance to the low-carbon transformation in various fields.

[0003] The green attributes of green methanol mainly depend on the renewability of the raw materials. Currently, there are two main recognized production routes for green methanol. The first route is the "electricity-to-methanol" route, which directly synthesizes green methanol by combining green carbon dioxide with green hydrogen, where green hydrogen comes from the electrolysis of water using green electricity, and green carbon dioxide comes from atmospheric capture or biomass energy. The second route is the "biomethanol" route, which uses biomass gasification to prepare raw gas, and the raw gas to synthesize green methanol. The "electricity-to-methanol" route is limited by the electrolysis and storage and transportation of green hydrogen, and needs to be built in areas with rich wind and solar resources. At the same time, the high cost of capturing renewable carbon dioxide also limits the application scenarios of this technology. The "biomethanol" route is limited by the maturity and large-scale nature of biomass gasification technology. At the same time, the characteristics of biomass resources such as wide distribution and low energy density make its storage and transportation system difficult and costly, making it difficult to achieve the scale effect of this technology.

[0004] However, the system for preparing green methanol has the following defects when used: 1. In the existing system for preparing green methanol, conventional technology usually combines hydrogen produced by renewable energy with carbon dioxide produced by renewable energy to synthesize green methanol. In this technology, carbon dioxide must be produced from renewable energy, which limits its scale and application. At the same time, it consumes more green hydrogen, and the investment and operating costs are high. In addition, the biomass green methanol synthesis unit has restrictions on impurities and inert components in the raw gas, which determines that biomass gasification must adopt pure oxygen gasification to reduce the content of inert components in the raw gas. However, biomass has the characteristics of high alkali metals and low ash melting point. The use of pure oxygen gasification can easily cause its ash to melt, leading to reactor blockage, failure, etc., which in turn affects the stable operation of the system; 2. In the existing system for preparing green methanol, distillation of the preparation material is an important step. In traditional solutions, the improvement of distillation quality is mainly achieved through the diversion of gas and liquid (gas upward, liquid downward) and the contact range of the filler (for distillation). However, when distilling materials in traditional methanol distillation towers, the downward diversion of liquid easily blocks the upward drift of gas, affecting the normal separation of gas and liquid during the distillation process. At the same time, the contact range between the filler used for distillation and the material is small, resulting in poor distillation effect on the material. Summary of the Invention

[0005] The object of the present invention is to provide a system and method for preparing green methanol from biomass to solve the problems raised in the above background technology.

[0006] In order to achieve the above-mentioned object of the invention, the present invention adopts the following technical solutions: The present invention provides a system for preparing green methanol from biomass, comprising: a biomass liquefaction unit and a green methanol unit, wherein the green methanol unit comprises: a methanol distillation tower, wherein a gas-liquid guide assembly is provided at the center of the methanol distillation tower, and an automated gas-liquid distillation mechanism is provided on both the upper and lower sides of the gas-liquid guide assembly. The automated gas-liquid distillation mechanism includes: a first driving source installed outside the methanol distillation tower; a driving shaft connected to the output end of the first driving source; a rotating disk connected to the driving shaft; a rotating arm rotatably connected to the eccentric side of the rotating disk; a gas circulation reciprocating assembly rotatably connected to the rotating arm; a tooth circulation assembly rotatably connected to the rotating arm; and a plurality of distillation brackets arranged outside the tooth circulation assembly and installed inside the methanol distillation tower. There are multiple rotating disks, rotating arms and tooth circulation components. Rotating disks are provided on the upper and lower sides of one rotating arm, and the bottom of the rotating disk at the bottom is connected to another rotating disk through a connecting rod.

[0007] As a preferred embodiment of the present invention, the biomass liquefaction unit includes: a heat carrier heating and lifting reactor; a heat carrier storage bin connected to the heat carrier heating and lifting reactor; a biomass liquefaction reactor connected to the heat carrier storage bin; a raw material bin connected to the biomass liquefaction reactor; a solid-solid separation device connected to the biomass liquefaction reactor; and a spray condensation device connected to the biomass liquefaction reactor. Among them, the heat carrier heating and lifting reactor is connected to the air preheater, the biomass liquefaction reactor is also connected to the heat carrier heating and lifting reactor, the side of the spray condensing device is connected to the green methanol unit, and the spray condensing device is also connected to the heat carrier heating and lifting reactor through the biomass gas blower.

[0008] As a preferred embodiment of the present invention, the green methanol unit further comprises: a biomass liquid pressure pump; a biomass liquid pure oxygen conversion device connected to the biomass liquid pressure pump; a waste heat boiler connected to the biomass liquid pure oxygen conversion device; a synthesis gas washing tower connected to the waste heat boiler; a conversion device connected to the synthesis gas washing tower; a desulfurization device connected to the conversion device; a decarbonization device connected to the desulfurization device; a raw gas preheating device connected to the decarbonization device; a methanol synthesis device connected to the raw gas preheating device; and a methanol distillation tower connected to the methanol synthesis device. The methanol synthesis device is also connected to the raw gas preheating device through a circulating gas compressor, the biomass liquid pure oxygen conversion device is also connected to the air separation system, and the biomass liquid pressure pump is connected to the spray condensation device.

[0009] As a preferred embodiment of the present invention, the methanol distillation tower consists of a lower tower body, a lower tower body, a middle tower body and an upper tower body. The top of the lower tower body is fixed with the lower tower body by screws, the top of the lower tower body is fixed with the middle tower body by screws, and the top of the middle tower body is fixed with the upper tower body by screws. Among them, the interior of the middle tower body is provided with a gas-liquid diversion component, the interiors of the lower tower body and the upper tower body are provided with an automatic gas-liquid distillation mechanism, and the interior of the lower tower body is provided with a distillation module.

[0010] As a preferred embodiment of the present invention, the gas-liquid guide assembly includes: a middle guide plate arranged inside the middle tower body; a side flow port opened at the angle of the side of the middle guide plate; an annular baffle installed on the outside of the top of the middle guide plate; an upper guide plate arranged on the top of the annular baffle and abutting against the top of the middle guide plate; a gas guide pipe arranged outside the annular baffle and passing through the middle tower body. Wherein, a plurality of gas ports are provided on one side of the middle guide plate located outside the annular baffle, and the gas guide pipe extends to the top of the upper guide plate.

[0011] As a preferred embodiment of the present invention, a plurality of liquid channels are installed on one side of the middle guide plate located inside the annular baffle, a cross bracket is installed on the inner top of the liquid channel, an intermediate slide rod is slidably connected to the inner part of the cross bracket, a conical umbrella body is installed on the top of the intermediate slide rod, and the conical umbrella body is arranged on the outer side of the top of the liquid channel. There is a gap between the inner wall of the conical umbrella body and the outer wall of the liquid channel, and a return spring installed between the cross bracket and the conical umbrella body is provided on the outer side of the middle slide bar.

[0012] As a preferred embodiment of the present invention, the gas circulation reciprocating assembly includes: an intermediate slide rotatably connected to the outside of the bottom of the rotating arm and extending through the lower tower body; an inner groove provided at the center of the inner portion of the intermediate slide; a plurality of horizontal slides slidably connected to the inner grooves; a gas nozzle installed at the center of the inner portion of the horizontal slide; a gas conduit connected to the gas nozzle and extending to the outside of the lower tower body; and an air pump connected to the gas conduit and installed on the outside of the lower tower body. Among them, telescopic springs connected to the inner wall of the inner groove are installed on the side surfaces of the horizontal slides on the left and right sides, and the air pump extends to the inner bottom of the lower tower body through another gas conduit connected to the bottom.

[0013] As a preferred embodiment of the present invention, the tooth circulation assembly includes: a horizontal sliding rod rotatably connected to the outside of the bottom of the rotating arm and extending to the bottom of the distillation bracket; a tooth plate installed on the top of the horizontal sliding rod; a movable gear meshingly connected to the side of the tooth plate; an eccentric rotating rod connected to the movable gear and rotatably connected to the inside of the distillation bracket; a side cam rod installed on the outside of the eccentric rotating rod; a vertical plate installed on the side of the side cam rod; and a plurality of movable rotating rods rotatably connected to the inside of the vertical plate.

[0014] As a preferred embodiment of the present invention, the inner center of the distillation support is set to be hollow, and the hollow part of the distillation support is provided with a plurality of distillation fillers, and a plurality of gas delivery conduits are installed at the inner edge of the distillation support, and the gas delivery conduits are located outside the distillation fillers.

[0015] The present invention also provides a method for preparing green methanol from biomass, comprising the following steps: S1. With the green methanol unit as the core, one or more biomass liquefaction units are constructed in a distributed manner according to the surrounding biomass raw materials. Biomass is converted into biomass liquid in the biomass liquefaction plant, and the biomass liquid is centrally transported to the green methanol plant for the production of green methanol. S2. The biomass raw materials in the raw material bin and the high-temperature heat carrier in the heat carrier storage bin are simultaneously fed into the biomass liquefaction reactor in proportion for pyrolysis and liquefaction reaction to obtain gaseous products and solid-phase products. The gaseous products are cooled by the spray condensation device to obtain biomass liquid and biomass gas. The biomass gas is transported by the biomass gas blower to the heat carrier heating and lifting reactor for system energy supply. The biomass liquid is transported to the green methanol unit, and the solid-phase products are separated by the solid-solid separation device to obtain biochar and solid heat carrier. The solid heat carrier is returned to the heat carrier heating and lifting reactor, and the biochar is separated, cooled, and shipped out. S3. After being pressurized by the biomass liquid booster pump, the biomass liquid enters the biomass liquefaction reactor together with oxygen for pure oxygen gasification reaction to obtain crude synthesis gas, where the oxygen comes from the air separation system. The crude synthesis gas is cooled in the waste heat boiler, washed and impurities removed by the synthesis gas scrubber, converted and adjusted for hydrogen-carbon ratio by the conversion device, desulfurized by the desulfurization device, and decarbonized by the decarbonization device to obtain raw gas. The raw gas is preheated by the raw gas preheating device and enters the methanol synthesis device and the methanol distillation tower to obtain green methanol. The circulating gas discharged from the methanol synthesis device is compressed and pressurized by the circulating gas compressor and then enters the raw gas preheating device together with the fresh raw gas. Compared with the existing technology, one or more of the above technical solutions have the following beneficial effects: 1) Adopting a distributed biomass liquefaction and centralized green methanol synthesis technology route will solve the difficulties and costs of biomass collection, storage and transportation, reduce the demand for chemical land, and realize the scale effect of green methanol plants; 2) Biomass is converted into biomass liquid by biomass liquefaction, and the biomass liquid is gasified with pure oxygen to prepare raw gas. The system completely avoids the situation of biomass ash melting, which can ensure the continuous and stable operation of the process system.

[0016] 1. In the system and method for producing green methanol from biomass, the operation of the first driving source can, on the one hand, drive the multiple gas nozzles for circulating gas to reciprocate (horizontally), so that the gas ejected from the gas nozzles can move in a spiral pattern to the inner top of the methanol distillation tower, and cause the gas at the top of the methanol distillation tower to circulate (with a certain intensity), thereby improving the efficiency of gas emission. On the other hand, it can drive the packing inside the distillation support to circulate, ensuring that the packing inside the distillation support expands the direct contact area between the packing and the liquid material during distillation and purification of the material (liquid) (removing impurities within it), thereby improving the packing's effectiveness and ability in distilling the liquid material. 2. In the system and method for producing green methanol from biomass, when the liquid material is distilled, the falling liquid material and the rising gas (distilled) will fall and rise respectively in the middle part of the distillation support and the middle guide plate, and at the edge of the distillation support and the middle guide plate, respectively, achieving separate liquid falling and gas rising operations, improving the effect and efficiency of distilling the material (liquid) and reducing the probability of the rising gas re-contacting the (falling) liquid. At the same time, the gas port and gas delivery conduit that guide the gas will not be disturbed or affected by the falling liquid, ensuring the ability to distill the methanol material and avoiding the problem of gas accumulation and difficulty in discharge. 3. In the system and method for producing green methanol from biomass, with the green methanol plant as the core, a distributed biomass liquefaction plant is constructed based on the surrounding biomass raw material storage conditions. The biomass is used to produce biomass liquid at the liquefaction plant, and the biomass liquid is centrally transported to the green methanol plant. This method, which uses "distributed construction of biomass liquefaction plants + centralized transportation of biomass liquid to the green methanol plant to synthesize green methanol," can effectively reduce the difficulty and cost of collecting, storing, and transporting biomass raw materials. Furthermore, the land used for the biomass liquefaction plant is general industrial land, while the land used for the green methanol plant is chemical land. Separate construction can significantly reduce the project's industrial land demand and land costs. 4. In the system and method for producing green methanol from biomass, biomass liquefaction technology is used to convert biomass into bioliquid. The bioliquid can be pressurized to the target pressure for methanol synthesis using only a pressure pump. Compared with conventional biomass gasification processes, this eliminates the need for syngas compression, resulting in a simpler process and greater energy savings. Simultaneously, the biomass is converted into bioliquid, effectively separating the ash from the biomass into biochar. The bioliquid contains virtually no ash, and the gasification process avoids ash melting or slagging, resulting in a more stable system and a simpler process. Furthermore, the system can operate independently or be combined with renewable energy hydrogen production processes, providing enhanced system flexibility. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The accompanying drawings, which constitute a part of the present invention, are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute improper limitations on the present invention.

[0018] Furthermore, the terms "installed," "disposed," "provided with," "connected," "connected," and "socketed" should be interpreted broadly. For example, they can refer to fixed connections, removable connections, or integral structures; mechanical connections or electrical connections; direct connections, indirect connections through an intermediary, or internal communication between two devices, elements, or components. Those skilled in the art will understand the specific meanings of these terms in this application based on the specific circumstances.

[0019] Figure 1 It is a structural schematic diagram of the green methanol production system of the present invention; Figure 2 This is a schematic structural diagram of the present invention using a new energy hydrogen production system to produce green methanol; Figure 3 Schematic diagram of the structure of the methanol distillation tower of the present invention; Figure 4 It is a schematic structural diagram of a cross-section of a methanol distillation tower of the present invention; Figure 5 This invention Figure 4 Schematic diagram of the structure of the enlarged area A in the middle; Figure 6 This is a schematic structural diagram of a front cross-sectional view of a methanol distillation tower according to the present invention; Figure 7 This is a structural schematic diagram of the cross-section of the connection between the lower tower body and the automated gas-liquid distillation mechanism of the present invention; Figure 8 It is a structural schematic diagram of the automated gas-liquid distillation mechanism of the present invention; Figure 9 This is a schematic structural diagram of the connection between the first driving source and the intermediate slide plate of the present invention; Figure 10 Schematic diagram of the structure of the gas circulation reciprocating assembly of the present invention; Figure 11 It is a schematic structural diagram of the tooth circulation assembly of the present invention; Figure 12 This is a schematic structural diagram of a cross-sectional view of the connection between the gas circulation reciprocating assembly and the distillation support of the present invention; Figure 13 This is a structural diagram of the cross-section of the connection between the middle tower body and the gas-liquid guide assembly of the present invention; Figure 14 It is a schematic structural diagram of a cross-section of the gas-liquid guide assembly of the present invention; Figure 15 This is a schematic structural diagram of a cross-sectional view of the connection between the liquid channel and the conical umbrella body of the present invention; Figure 16 This is a schematic structural diagram of a cross-sectional view of the connection between a gas delivery conduit and a cylindrical sleeve according to the present invention; Figure 17 is a schematic diagram of the green methanol plant of the present invention; In the picture: 1. Biomass liquefaction unit; 101. Heat carrier heating and lifting reactor; 102. Heat carrier storage bin; 103. Raw material bin; 104. Biomass liquefaction reactor; 105. Air preheater; 106. Solid-solid separation device; 107. Biomass air blower; 108. Spray condensation device; 2. Green methanol unit; 201. Biomass liquid pressure pump; 202. Biomass liquid pure oxygen conversion unit; 203. Waste heat boiler; 204. Synthesis gas scrubber; 205. Conversion unit; 206. Desulfurization unit; 207. Decarbonization unit; 208. Feed gas preheating unit; 209. Methanol synthesis unit; 211. Recycle gas compressor; 212. Air separation system; 3. New energy hydrogen production system; 301. Photovoltaic power generation device; 302. Wind power generation device; 303. Electrolytic hydrogen production device; 304. Oxygen compressor; 305. Oxygen storage tank; 306. Hydrogen compressor; 307. Hydrogen storage tank; 10. Methanol distillation tower; 1001. Lower tower body; 10011. Distillation module; 1002. Lower tower body; 1003. Middle tower body; 1004. Upper tower body; 20. Gas-liquid guide assembly; 2001. Central guide plate; 20011. Gas port; 20012. Liquid channel; 20013. Cross bracket; 20014. Middle slide bar; 20015. Conical umbrella body; 20016. Return spring; 2002. Side flow port; 2003. Annular baffle; 2004. Upper guide plate; 2005. Gas guide tube; 30. Automated gas-liquid distillation mechanism; 3001. First drive source; 3002. Drive shaft; 3003. Rotating disk; 30031. Connecting rod; 3004. Rotating arm; 3005. Gas circulation reciprocating assembly; 3006. Tooth circulation assembly; 3007. Distillation support; 30071. Gas delivery conduit; 3051, middle slide; 3052, inner groove; 3053, horizontal slide; 30531, telescopic spring; 3054, gas nozzle; 3055, gas duct; 3056, air pump; 3061, horizontal slide bar; 3062, tooth plate; 3063, movable gear; 3064, eccentric rotating rod; 3065, side convex rod; 3066, vertical plate; 3067, movable rotating rod; 40. Cross assembly bracket; 401. Cylindrical sleeve; 402. One-way air valve; 403. Air outlet. DETAILED DESCRIPTION

[0020] In order to enable those skilled in the art to better understand the present invention, the following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments in the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts should fall within the scope of protection of this application. Example 1

[0021] See also Figures 1-15 A system for preparing green methanol from biomass includes a biomass liquefaction unit 1 and a green methanol unit 2. The green methanol unit 2 includes: a methanol distillation tower 10, a gas-liquid guide assembly 20 is provided at the center of the interior of the methanol distillation tower 10, and an automatic gas-liquid distillation mechanism 30 is provided on both the upper and lower sides of the gas-liquid guide assembly 20. The automatic gas-liquid distillation mechanism 30 includes: a first driving source 3001 installed on the outside of the methanol distillation tower 10; a driving shaft 3002 connected to the output end of the first driving source 3001; a rotating disk 3003 connected to the driving shaft 3002; and a rotating disk 3003 connected to the side of the rotating disk 3003. A rotating arm 3004 at an eccentric position; a gas circulation reciprocating assembly 3005 rotatably connected to the rotating arm 3004; a tooth circulation assembly 3006 rotatably connected to the rotating arm 3004; a plurality of distillation supports 3007 arranged on the outside of the tooth circulation assembly 3006 and installed inside the methanol distillation tower 10, wherein a plurality of rotating disks 3003, rotating arms 3004 and tooth circulation assemblies 3006 are provided, and rotating disks 3003 are provided on the upper and lower sides of a rotating arm 3004, and the bottom of the rotating disk 3003 at the bottom is connected to another rotating disk 3003 through a connecting rod 30031.

[0022] In the present invention, the methanol distillation tower 10 consists of a lower tower body 1001, a lower tower body 1002, a middle tower body 1003 and an upper tower body 1004. The top of the lower tower body 1001 is installed with the lower tower body 1002 by screws, the top of the lower tower body 1002 is installed with the middle tower body 1003 by screws, and the top of the middle tower body 1003 is installed with the upper tower body 1004 by screws, wherein the interior of the middle tower body 1003 is provided with a gas-liquid diversion component 20, the interior of the lower tower body 1002 and the upper tower body 1004 are provided with an automated gas-liquid distillation mechanism 30, and the interior of the lower tower body 1001 is provided with a distillation module 10011.

[0023] The operating principle is as follows: When distilling the material delivered to the methanol distillation column 10, the first drive source 3001 is activated, driving the drive shaft 3002 and the rotating disk 3003 connected to the output end of the first drive source 3001 to rotate. As the rotating disk 3003 rotates, the rotating arm 3004, which is rotatably connected to the eccentric portion of the rotating arm 3004, activates. This causes the gas reciprocating assembly 3005, which is rotatably connected to the outer portion of the rotating arm 3004, to reciprocate the circulating gas. This causes the circulating gas to be transported in a spiral pattern within the methanol distillation column 10 to the inner tops of the lower tower body 1002 and the upper tower body 1004, thereby enhancing the gas's mobility within the methanol distillation column 10. Simultaneously, the operation of the rotating arm 3004 also drives the tooth circulation assembly 3006, which activates the packing inside the distillation support 3007, which performs the distillation operation, thereby increasing the contact area between the packing and the material (liquid) and the distillation efficiency.

[0024] In the present invention, the internal structure of the gas-liquid guiding component 20 is designed so that the liquid falls in the middle and the gas rises at the edge, and the two activities are carried out separately, thereby improving the gas-liquid guiding capability.

[0025] Specific reference Figure 1 The biomass liquefaction unit 1 includes: a heat carrier heating and lifting reactor 101; a heat carrier storage bin 102 connected to the heat carrier heating and lifting reactor 101; a biomass liquefaction reactor 104 connected to the heat carrier storage bin 102; a raw material bin 103 connected to the biomass liquefaction reactor 104; a solid-solid separation device 106 connected to the biomass liquefaction reactor 104; and a spray condensation device 108 connected to the biomass liquefaction reactor 104, wherein the heat carrier heating and lifting reactor 101 is connected to the air preheater 105, and the biomass liquefaction reactor 104 is also connected to the heat carrier heating and lifting reactor 101. The side of the spray condensation device 108 is connected to the green methanol unit 2, and the spray condensation device 108 is also connected to the heat carrier heating and lifting reactor 101 through a biomass gas blower 107.

[0026] In the present invention, the methanol distillation tower 10 consists of a lower tower body 1001, a lower tower body 1002, a middle tower body 1003 and an upper tower body 1004. The top of the lower tower body 1001 is installed with the lower tower body 1002 by screws, the top of the lower tower body 1002 is installed with the middle tower body 1003 by screws, and the top of the middle tower body 1003 is installed with the upper tower body 1004 by screws, wherein the interior of the middle tower body 1003 is provided with a gas-liquid diversion component 20, the interior of the lower tower body 1002 and the upper tower body 1004 are provided with an automated gas-liquid distillation mechanism 30, and the interior of the lower tower body 1001 is provided with a distillation module 10011.

[0027] Specific reference Figure 1 and Figure 2 The green methanol unit 2 also includes: a biomass liquid pressure pump 201; a biomass liquid pure oxygen conversion device 202 connected to the biomass liquid pressure pump 201; a waste heat boiler 203 connected to the biomass liquid pure oxygen conversion device 202; a synthesis gas washing tower 204 connected to the waste heat boiler 203; a conversion device 205 connected to the synthesis gas washing tower 204; a desulfurization device 206 connected to the conversion device 205; a decarbonization device 207 connected to the desulfurization device 206; a raw gas preheating device 208 connected to the decarbonization device 207; a methanol synthesis device 209 connected to the raw gas preheating device 208; and a methanol distillation tower 10 connected to the methanol synthesis device 209, wherein the methanol synthesis device 209 is also connected to the raw gas preheating device 208 via a circulating gas compressor 211, the biomass liquid pure oxygen conversion device 202 is also connected to the air separation system 212, and the biomass liquid pressure pump 201 is connected to the spray condensation device 108.

[0028] Specific reference Figure 13 、 Figure 14 and Figure 15 The gas-liquid guide assembly 20 includes: a central guide plate 2001 arranged inside the central tower body 1003; a side flow port 2002 opened at the side angle of the central guide plate 2001; an annular baffle 2003 installed on the outside of the top of the central guide plate 2001; an upper guide plate 2004 arranged on the top of the annular baffle 2003 and abutting the top of the central guide plate 2001; a gas guide pipe 2005 arranged outside the annular baffle 2003 and passing through the central tower body 1003, wherein a plurality of gas ports 20011 are opened on one side of the central guide plate 2001 located outside the annular baffle 2003, and the gas guide pipe 2005 extends to the top of the upper guide plate 2004.

[0029] In this solution, a plurality of liquid channels 20012 are installed on one side of the middle guide plate 2001 located inside the annular baffle 2003, a cross bracket 20013 is installed on the inner top of the liquid channel 20012, an intermediate slide bar 20014 is slidably connected to the inside of the cross bracket 20013, a conical umbrella body 20015 is installed on the top of the intermediate slide bar 20014, and the conical umbrella body 20015 is arranged on the outside of the top of the liquid channel 20012, wherein a gap is left between the inner wall of the conical umbrella body 20015 and the outer wall of the liquid channel 20012, and a return spring 20016 is provided on the outside of the intermediate slide bar 20014 and installed between the cross bracket 20013 and the conical umbrella body 20015.

[0030] In the biomass-to-green methanol system of the present invention, when liquid material is diverted, the falling liquid first contacts upper guide plate 2004 and falls through upper guide plate 2004, which abuts the inner wall of middle guide plate 2001, into middle guide plate 2001. The liquid (material) then flows into middle guide plate 2001 through the gap between conical body 20015 and liquid channel 20012, entering liquid channel 20012 and discharging from within liquid channel 20012 to the bottom of middle guide plate 2001. A return spring 20016, positioned between cross support 20013 and conical body 20015, supports the position of conical body 20015, ensuring that the bottom of conical body 20015 does not obstruct the top opening of liquid channel 20012, thus ensuring smooth liquid flow. Among them, the design of the annular baffle 2003, on the one hand, expands the space for temporary storage of liquid at the top of the middle guide plate 2001, and on the other hand, separates the space at the top of the gas port 20011 where gas flows and the space for temporary storage of liquid on the middle guide plate 2001, ensuring that the gas and liquid diversion will not conflict.

[0031] Specific reference Figure 8 、 Figure 9 and Figure 10The gas circulation reciprocating assembly 3005 includes: an intermediate slide 3051 rotatably connected to the outer side of the bottom of the rotating arm 3004 and arranged through the lower tower body 1002; an inner groove 3052 opened at the center of the intermediate slide 3051; a plurality of horizontal slides 3053 slidably connected to the inner groove 3052; a gas nozzle 3054 installed at the center of the horizontal slide 3053; a gas duct 3055 connected to the gas nozzle 3054 and extending to the outside of the lower tower body 1002; and an air pump 3056 connected to the gas duct 3055 and installed on the outside of the lower tower body 1002, wherein the sides of the horizontal slides 3053 on the left and right sides are equipped with telescopic springs 30531 connected to the inner wall of the inner groove 3052, and the air pump 3056 extends to the inner bottom of the lower tower body 1002 through another gas duct 3055 connected to the bottom.

[0032] In the biomass-based green methanol production system of the present invention, when the rotating arm 3004 is in operation, the intermediate slide 3051, which is rotatably connected to the intermediate slide 3051, reciprocates under the action of the lower tower body 1002 (sliding connection), driving the horizontal slide 3053 mounted inside the intermediate slide 3051 to reciprocate (horizontally). When the horizontal slide 3053 and the intermediate slide 3051 collide, the horizontal slide 3053 is pushed to slide within the inner groove 3052, changing the position of the multiple horizontal slides 3053 and the internal gas nozzle 3054. In conjunction with the reciprocating movement of the gas nozzle 3054, the ejected gas is formed into a spiral shape. The gas at the bottom of the lower tower body 1002 is pumped into the interior of the gas nozzle 3054 through the gas conduit 3055 by the air pump 3056, thus achieving gas diversion.

[0033] Specific reference Figure 8 、 Figure 9 and Figure 11 The tooth circulation assembly 3006 includes: a horizontal sliding bar 3061 rotatably connected to the outside of the bottom of the rotating arm 3004 and extending to the bottom of the distillation bracket 3007; a tooth plate 3062 installed on the top of the horizontal sliding bar 3061; a movable gear 3063 meshingly connected to the side of the tooth plate 3062; an eccentric rotating rod 3064 connected to the movable gear 3063 and rotatably connected to the inside of the distillation bracket 3007; a side protrusion rod 3065 installed on the outside of the eccentric rotating rod 3064; a vertical plate 3066 installed on the side of the side protrusion rod 3065; and a plurality of movable rotating rods 3067 rotatably connected to the inside of the vertical plate 3066.

[0034] In the biomass-to-green methanol system of the present invention, when the rotating arm 3004 operates, the horizontal slide 3061, rotatably connected to it, reciprocates under the action of the lower tower body 1002 (sliding connection), driving the toothed plate 3062 mounted on top of the horizontal slide 3061 to move (horizontally reciprocate). As the toothed plate 3062 moves, the movable gear 3063 meshing with its side rotates, causing the eccentric rotating rod 3064 mounted inside the movable gear 3063 to rotate. This causes the outer side of the eccentric rotating rod 3064 to rotate (from 0 to 180 degrees) via the side protrusions 3065 and the vertical plate 3066. As the vertical plate 3066 rotates, the multiple movable rotating rods 3067 movably connected to it rotate longitudinally and vertically (simultaneously), driving the packing inside the distillation support 3007 to move, increasing the contact area between the packing and the material and improving the distillation capacity.

[0035] Specific reference Figure 12 The inner center of the distillation support 3007 is set to be hollow, and the hollow part of the distillation support 3007 is provided with a number of distillation fillers. A plurality of gas delivery conduits 30071 are installed at the inner edge of the distillation support 3007, and the gas delivery conduits 30071 are located outside the distillation fillers.

[0036] In the system for preparing green methanol from biomass of the present invention, the design of the gas delivery conduit 30071 ensures that the distillation of the liquid and the wafting of the gas can be carried out separately. Example 2

[0037] During use, it was discovered that when gas delivery conduit 30071 is used as a passage for gas flow, its top must be open. In this case, the liquid (material) being distilled can easily fall into gas delivery conduit 30071, blocking and disrupting the normal flow of gas therein, thus affecting its normal flow and movement.

[0038] For this purpose, refer specifically to Figure 16 A cross-assembly bracket 40 is installed at the inner top of the gas delivery conduit 30071. A cylindrical sleeve 401 is installed at the eccentric point of the top of the cross-assembly bracket 40 through a support rod. A one-way gas valve 402 is installed at the center of the cylindrical sleeve 401, wherein an air outlet 403 is left between the inner wall of the cylindrical sleeve 401 and the outer wall of the gas delivery conduit 30071.

[0039] In the biomass-based green methanol production system of the present invention, the design of cylindrical sleeve 401 ensures that falling liquid first contacts cylindrical sleeve 401 and does not fall into the interior of gas delivery conduit 30071. This allows the flow of gas and the fall of liquid to proceed independently without conflict or interference. Furthermore, the design of gas outlet 403 ensures that the gas is not disturbed when it moves to the inner top of methanol distillation column 10. One-way valve 402 is operable to ensure that gas can move from the interior of cylindrical sleeve 401 to the outside, preventing external liquid from entering the interior of cylindrical sleeve 401. Example 3

[0040] Specific reference Figure 2 The present invention provides a system for preparing green methanol from biomass, and a new energy hydrogen production system 3 can be introduced, including: a photovoltaic power generation device 301, a wind power generation device 302, an electrolytic hydrogen production device 303, an oxygen compressor 304, an oxygen storage tank 305, a hydrogen compressor 306 and a hydrogen storage tank 307.

[0041] Among them, in the new energy hydrogen production system 3: green electricity can come from one or more of the photovoltaic power generation device 301 and the wind power generation device 302; the electrolytic hydrogen production device 303 is directly connected to the oxygen compressor 304 and the oxygen storage tank 305; the electrolytic hydrogen production device 303 is directly connected to the hydrogen compressor 306 and the hydrogen storage tank 307.

[0042] Furthermore, the oxygen storage tank 305 is directly connected to the biomass liquid pure oxygen conversion device 202; and the hydrogen storage tank 307 is directly connected to the raw gas preheating device 208. Example 4

[0043] See also Figures 1-15 A method for preparing green methanol from biomass comprises the following steps: S1. With the green methanol unit as the core, one or more biomass liquefaction units are constructed in a distributed manner according to the surrounding biomass raw materials. Biomass is converted into biomass liquid in the biomass liquefaction plant, and the biomass liquid is centrally transported to the green methanol plant for the production of green methanol. S2, the biomass raw materials in the raw material warehouse 103 and the high-temperature heat carrier in the heat carrier storage bin 102 are simultaneously fed into the biomass liquefaction reactor 104 in proportion for pyrolysis and liquefaction reaction to obtain gaseous products and solid-phase products. The gaseous products are cooled by the spray condensation device 108 to obtain biomass liquid and biomass gas. The biomass gas is transported by the biomass gas blower 107 to the heat carrier heating and lifting reactor 101 for system energy supply. The biomass liquid is transported into the green methanol unit 2, and the solid-phase products enter the solid-solid separation device 106 for separation to obtain biochar and solid heat carrier. The solid heat carrier is returned to the heat carrier heating and lifting reactor 101, and the biochar is separated, cooled, and shipped out; S3. After being pressurized by the biomass liquid pressure pump 201, the biomass liquid enters the biomass liquefaction reactor 104 together with oxygen for pure oxygen gasification reaction to obtain crude synthesis gas, wherein the oxygen comes from the air separation system 212. The crude synthesis gas is cooled in the waste heat boiler 203, washed and impurities removed by the synthesis gas washing tower 204, converted and adjusted the hydrogen-carbon ratio by the conversion device 205, desulfurized by the desulfurization device 206, and decarbonized by the decarbonization device 207 to obtain raw gas. The raw gas is preheated by the raw gas preheating device 208 and enters the methanol synthesis device 209 and the methanol distillation tower 10 to obtain green methanol. The circulating gas discharged from the methanol synthesis device 209 is compressed and pressurized by the circulating gas compressor 211 and enters the raw gas preheating device 208 together with the fresh raw gas. Example 5

[0044] Specific reference Figure 2 and Figure 17 A method for preparing green methanol from biomass also includes: the system for preparing green methanol from biomass can be coupled with a new energy hydrogen production system 3, and renewable green electricity generated by wind energy, photovoltaics, etc. is used to electrolyze water to produce hydrogen to obtain high-purity hydrogen and oxygen, which are compressed by a hydrogen compressor 306 and an oxygen compressor 304 and stored in a hydrogen storage tank 307 and an oxygen storage tank 305 respectively; the biomass liquid is pressurized by a biomass liquid pressure pump 201 and enters a biomass liquefaction reactor 104 together with oxygen for a pure oxygen gasification reaction to obtain a crude synthesis gas, where the oxygen comes from the oxygen storage tank 305; the crude synthesis gas is cooled in a waste heat boiler 203, washed and impurity-removed in a synthesis gas washing tower 204, desulfurized in a desulfurization device 206, and hydrogen is added to adjust the hydrogen-to-carbon ratio to obtain a raw gas, where the hydrogen comes from the hydrogen storage tank 307; the raw gas is preheated by a raw gas preheating device 208 and enters a methanol synthesis device 209 and a methanol distillation tower 10 to obtain green methanol. The circulating gas discharged from the methanol synthesis unit 209 is compressed and pressurized by the circulating gas compressor 211 and then enters the raw gas preheating device 208 together with the fresh raw gas.

[0045] Furthermore, the biomass raw material can be one or more of agricultural wastes such as straw and rice husk, woody forestry waste, livestock manure, organic waste, etc., with a raw material particle size of 0.5 to 30 mm; Further, the heat carrier may be sand, ceramics, ore, cinder, slag, molecular sieves and the like one or more, particle size 0.5 ~ 5mm; Furthermore, the temperature of the biomass liquefaction reactor 104 is 450-900°C, preferably, the temperature of the biomass liquefaction reactor 104 is 550-750°C; Furthermore, the pressure of the biomass liquefaction reactor 104 is 0.1 to 100 kPa, preferably, the pressure of the biomass liquefaction reactor 104 is 3 to 10 kPa; Furthermore, the mass ratio of the heat carrier to the biomass raw material is 5:1 to 20:1, preferably, the mass ratio of the heat carrier to the biomass raw material is 8:1 to 12:1; Furthermore, the temperature of the biomass liquefaction reactor 104 is 1200-1450°C, preferably, the temperature of the biomass liquefaction reactor 104 is 1300-1350°C; Furthermore, the pressure of the biomass liquefaction reactor 104 is 0.1 to 10,000 kPa, preferably, the pressure of the biomass liquefaction reactor 104 is 5,500 to 6,500 kPa; Furthermore, the flue gas after heat exchange in the air preheater is used to dry the biomass raw materials. Example 6

[0046] Attached with instruction manual Figure 1 For example, rice husks are used as biomass raw materials, with a particle size of ≤3 mm and stored in raw material bin 103. Alumina molecular sieves are used as heat carriers, with a particle size of 2-3 mm and a mass ratio of alumina molecular sieve to rice husks of 10:1. The heat carrier is heated in elevating reactor 101 to a temperature of 820°C and then stored in heat carrier storage bin 102. The heat carrier and rice husks enter the system simultaneously for thorough mixing and mass and heat transfer. The pyrolysis temperature is 650°C and the reaction pressure is 4 kPa, producing gaseous and solid products. Among them, the solid phase product: biochar and heat carrier enter the biochar separation device together for separation, and biochar and heat carrier are obtained after separation. The biochar is stored and sold after cooling; the heat carrier enters the heat carrier heating and lifting reactor 101 for heating; the gas phase product (650℃) enters the spray condensation device 108 for spray cooling, and obtains biomass gas and biomass liquid, among which the biomass gas is transported to the heat carrier heating and lifting reactor 101 through the biomass gas fan 107 for heating and energy supply of the heat carrier; the flue gas and air are heat exchanged through the air preheater 105 to obtain preheated air of 220℃, which is used to heat the combustion oxygen supply of the heating and lifting reactor. After heat exchange, the flue gas is 600℃ and is used for rice husk drying after heat exchange and cooling. The biomass liquid is pumped via a biomass liquid booster pump 201 into a biomass liquid pure oxygen conversion unit 202 for a pure oxygen gasification reaction. Oxygen is provided by an air separation unit. The reaction temperature in the biomass liquid pure oxygen conversion unit 202 is 1350°C and the reaction pressure is 6 MPa. After cooling and purification in a waste heat boiler 203 and a syngas scrubber 204, reformed gas is obtained (dry gas volume fraction: CO: 43.64%, H2: 48.65%, CH4: 0.13%, CO2: 6.27%, and other: 1.31%). The crude syngas then enters a shift unit 205, a desulfurization unit 206, and a decarbonization unit 207 to remove sulfur impurities and carbon dioxide, producing a feed gas with a qualified hydrogen-to-carbon ratio (H2 / CO = 2.05 by volume). After being preheated to 200°C in a feed gas preheater 208, the feed gas enters a methanol synthesis unit 209 for methanol synthesis (reaction temperature: 225°C), producing green methanol. Example 7

[0047] Attached with instruction manual Figure 2 For example, green electricity generated by wind and solar energy is delivered to an electrolyzer for water electrolysis to produce hydrogen. The resulting hydrogen and oxygen are compressed to 6.0 MPa by hydrogen compressor 306 and oxygen compressor 604, respectively, before being stored in hydrogen storage tank 307 and oxygen storage tank 305. Wood chips are used as biomass raw material, with a particle size of ≤3 mm and stored in raw material bin 103. Ceramic beads are used as heat carrier, with a particle size of 2-3 mm and a mass ratio of 12:1. The heat carrier is heated to 810°C in heating reactor 101 and stored in heat carrier storage bin 102. The heat carrier and wood chips enter biomass liquefaction reactor 104 simultaneously for thorough mixing and mass and heat transfer. Pyrolysis is performed at a temperature of 660°C and a reaction pressure of 5 kPa, producing solid and gaseous products. Among them, the solid phase product biochar and the heat carrier enter the solid-solid separation device 106 together for separation, and biochar and heat carrier are obtained after separation. The biochar is stored and sold after cooling; the heat carrier enters the heating and lifting reactor 101 for heating; the gas phase product (660℃) enters the spray condensation device 108 for spray cooling to obtain biomass liquid and biomass gas, among which the biomass gas is transported to the heat carrier heating and lifting reactor 101 through the biomass gas fan 107 for heating and energy supply of the heat carrier; the flue gas and air are heat exchanged through the air preheater 105 to obtain preheated air of 220℃, which is used for combustion and oxygen supply of the heat carrier heating and lifting reactor 101. After heat exchange, the flue gas of 605℃ is used for sawdust drying after heat exchange and cooling. The biomass liquid is pumped via a biomass liquid booster pump 201 into a biomass liquid pure oxygen conversion unit 202 for a pure oxygen gasification reaction. Oxygen is provided by the water electrolysis hydrogen production unit. The reactor operates at a temperature of 1450°C and a pressure of 5.6 MPa. After cooling and purification in a waste heat boiler 203 and a syngas scrubber 204, a crude syngas (volume fractions: CO: 42.45%, H2: 50.49%, CH4: 0.10%, CO2: 5.75%, and other gases: 1.21%) is produced. The crude syngas is then fed directly into a desulfurization unit 206 to remove sulfur impurities, producing a crude feed gas. This feed gas is then mixed with hydrogen from the water electrolysis hydrogen production unit (H2 / CO = 2.05, by volume), preheated to 200°C in a feed gas preheater 208, and then fed into a methanol synthesis unit 209 for methanol synthesis (reaction temperature: 235°C), producing green methanol.

[0048] Without limitation, any person skilled in the art who is familiar with the technical field can make equivalent replacements or changes based on the technical solutions and inventive concepts of the present invention within the technical scope disclosed by the present invention, and these changes should be covered by the protection scope of the present invention.

Claims

1. A system for producing green methanol from biomass, characterized in that: include: A biomass liquefaction unit (1) and a green methanol unit (2), wherein the green methanol unit (2) comprises: a methanol distillation tower (10), a gas-liquid guide assembly (20) being provided at the center of the interior of the methanol distillation tower (10), and automatic gas-liquid distillation mechanisms (30) being provided on both the upper and lower sides of the gas-liquid guide assembly (20). The automated gas-liquid distillation mechanism (30) comprises: a first driving source (3001) installed outside the methanol distillation tower (10); a driving shaft (3002) connected to the output end of the first driving source (3001); a rotating disk (3003) connected to the driving shaft (3002); a rotating arm (3004) rotatably connected to an eccentric side of the rotating disk (3003); a gas circulation reciprocating assembly (3005) rotatably connected to the rotating arm (3004); a tooth circulation assembly (3006) rotatably connected to the rotating arm (3004); and a plurality of distillation supports (3007) arranged outside the tooth circulation assembly (3006) and installed inside the methanol distillation tower (10). The rotating disk (3003), the rotating arm (3004) and the tooth circulation assembly (3006) are each provided in plurality. A rotating disk (3003) is provided on both the upper and lower sides of one rotating arm (3004), and the bottom of the rotating disk (3003) located at the bottom is connected to another rotating disk (3003) via a connecting rod (30031).

2. The system for producing green methanol from biomass according to claim 1, characterized in that: The biomass liquefaction unit (1) comprises: a heat carrier heating and lifting reactor (101); a heat carrier storage bin (102) connected to the heat carrier heating and lifting reactor (101); a biomass liquefaction reactor (104) connected to the heat carrier storage bin (102); a raw material bin (103) connected to the biomass liquefaction reactor (104); a solid-solid separation device (106) connected to the biomass liquefaction reactor (104); and a spray condensation device (108) connected to the biomass liquefaction reactor (104). The heat carrier heating and lifting reactor (101) is connected to the air preheater (105), the biomass liquefaction reactor (104) is also connected to the heat carrier heating and lifting reactor (101), the side of the spray condensing device (108) is connected to the green methanol unit (2), and the spray condensing device (108) is also connected to the heat carrier heating and lifting reactor (101) through the biomass gas blower (107).

3. The system for producing green methanol from biomass according to claim 2, characterized in that: The green methanol unit (2) further comprises: a biomass liquid pressure pump (201); a biomass liquid pure oxygen conversion device (202) connected to the biomass liquid pressure pump (201); a waste heat boiler (203) connected to the biomass liquid pure oxygen conversion device (202); a synthesis gas washing tower (204) connected to the waste heat boiler (203); a conversion device (205) connected to the synthesis gas washing tower (204); a desulfurization device (206) connected to the conversion device (205); a decarbonization device (207) connected to the desulfurization device (206); a raw gas preheating device (208) connected to the decarbonization device (207); a methanol synthesis device (209) connected to the raw gas preheating device (208); and a methanol distillation tower (10) connected to the methanol synthesis device (209). The methanol synthesis device (209) is further connected to the raw gas preheating device (208) via a circulating gas compressor (211), the biomass liquid pure oxygen conversion device (202) is further connected to an air separation system (212), and the biomass liquid pressure pump (201) is connected to the spray condensation device (108).

4. The system for producing green methanol from biomass according to claim 1, characterized in that: The methanol distillation tower (10) consists of a lower tower body (1001), a lower tower body (1002), a middle tower body (1003), and an upper tower body (1004); the top of the lower tower body (1001) is mounted with the lower tower body (1002) via screws; the top of the lower tower body (1002) is mounted with the middle tower body (1003) via screws; and the top of the middle tower body (1003) is mounted with the upper tower body (1004) via screws. The middle tower body (1003) is provided with a gas-liquid diversion assembly (20), the lower tower body (1002) and the upper tower body (1004) are provided with an automated gas-liquid distillation mechanism (30), and the lower tower body (1001) is provided with a distillation module (10011).

5. The system for producing green methanol from biomass according to claim 4, characterized in that: The gas-liquid guide assembly (20) comprises: a middle guide plate (2001) arranged inside the middle tower body (1003); a side flow opening (2002) provided at a side angle of the middle guide plate (2001); an annular baffle (2003) installed outside the top of the middle guide plate (2001); an upper guide plate (2004) arranged on the top of the annular baffle (2003) and in contact with the top of the middle guide plate (2001); and a gas guide pipe (2005) arranged outside the annular baffle (2003) and penetrating the middle tower body (1003). The middle guide plate (2001) is provided with a plurality of gas ports (20011) on one side outside the annular baffle (2003), and the gas guide tube (2005) extends to the top of the upper guide plate (2004).

6. The system for producing green methanol from biomass according to claim 5, characterized in that: The middle guide plate (2001) is located on one side inside the annular baffle (2003) and is provided with a plurality of liquid channels (20012). A cross bracket (20013) is provided on the inner top of the liquid channel (20012). An intermediate slide bar (20014) is slidably connected to the interior of the cross bracket (20013). A conical umbrella body (20015) is provided on the top of the intermediate slide bar (20014). The conical umbrella body (20015) is provided on the outer side of the top of the liquid channel (20012). A gap is left between the inner wall of the conical umbrella body (20015) and the outer wall of the liquid channel (20012), and a return spring (20016) installed between the cross bracket (20013) and the conical umbrella body (20015) is provided on the outer side of the middle slide bar (20014).

7. The system for producing green methanol from biomass according to claim 4, characterized in that: The gas circulation reciprocating assembly (3005) comprises: an intermediate slide (3051) rotatably connected to the outer side of the bottom of the rotating arm (3004) and penetrating the lower tower body (1002); an inner groove (3052) provided at the inner center of the intermediate slide (3051); a plurality of horizontal slides (3053) slidably connected to the inner grooves (3052); a gas nozzle (3054) installed at the inner center of the horizontal slide (3053); a gas conduit (3055) connected to the gas nozzle (3054) and extending to the outside of the lower tower body (1002); and an air pump (3056) connected to the gas conduit (3055) and installed on the outer side of the lower tower body (1002). The sides of the horizontal slides (3053) on the left and right sides are provided with telescopic springs (30531) connected to the inner wall of the inner groove (3052), and the air pump (3056) extends to the inner bottom of the lower tower body (1002) through another gas conduit (3055) connected at the bottom.

8. The system for producing green methanol from biomass according to claim 4, characterized in that: The tooth circulation assembly (3006) includes: a horizontal sliding bar (3061) rotatably connected to the outside of the bottom of the rotating arm (3004) and extending to the bottom of the distillation support (3007); a tooth plate (3062) installed on the top of the horizontal sliding bar (3061); a movable gear (3063) meshingly connected to the side of the tooth plate (3062); an eccentric rotating rod (3064) connected to the movable gear (3063) and rotatably connected to the inside of the distillation support (3007); a side convex rod (3065) installed on the outside of the eccentric rotating rod (3064); a vertical plate (3066) installed on the side of the side convex rod (3065); and a plurality of movable rotating rods (3067) rotatably connected to the inside of the vertical plate (3066).

9. The system for producing green methanol from biomass according to claim 1, characterized in that: The inner center of the distillation support (3007) is set to be hollow, and a number of distillation fillers are set in the hollow part of the distillation support (3007). A plurality of gas delivery conduits (30071) are installed at the inner edge of the distillation support (3007), and the gas delivery conduits (30071) are located outside the distillation fillers.

10. A method for preparing green methanol from biomass, for a system for preparing green methanol from biomass according to any one of claims 1-9, characterized in that: The following steps are involved: S1. With the green methanol unit as the core, one or more biomass liquefaction units are constructed in a distributed manner according to the surrounding biomass raw materials. Biomass is converted into biomass liquid in the biomass liquefaction plant, and the biomass liquid is centrally transported to the green methanol plant for the production of green methanol. S2, the biomass raw materials in the raw material bin (103) and the high-temperature heat carrier in the heat carrier storage bin (102) enter the biomass liquefaction reactor (104) in proportion and simultaneously for pyrolysis and liquefaction reaction to obtain gas phase products and solid phase products, wherein the gas phase products are sprayed and condensed by the condensation device (108) for cooling to obtain biomass liquid and biomass gas, and the biomass gas is transported by the biomass gas blower (107) to the heat carrier heating and lifting reactor (101) for system energy supply, and the biomass liquid is transported to the green methanol unit (2), and the solid phase product enters the solid-solid separation device (106) for separation to obtain biomass charcoal and solid heat carrier, and the solid heat carrier is returned to the heat carrier heating and lifting reactor (101), and the biomass charcoal is separated, cooled and sent out; S3. The biomass liquid is pressurized by the biomass liquid pressure pump (201) and enters the biomass liquefaction reactor (104) together with oxygen for pure oxygen gasification reaction to obtain a crude synthesis gas, wherein the oxygen comes from the air separation system (212). The crude synthesis gas is cooled by the waste heat boiler (203), washed and impurity-removed by the synthesis gas washing tower (204), converted and adjusted for the hydrogen-carbon ratio by the conversion device (205), desulfurized by the desulfurization device (206), and decarbonized by the decarbonization device (207) to obtain the raw gas. The raw gas is preheated by the raw gas preheating device (208) and enters the methanol synthesis device (209) and the methanol distillation tower (10) to obtain green methanol. The circulating gas discharged from the methanol synthesis device (209) is compressed and pressurized by the circulating gas compressor (211) and enters the raw gas preheating device (208) together with the fresh raw gas.

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