Biomass green hydrogen poly-generation coupling system

Abstract

The invention relates to the field of low-carbon alcohol hydrogen storage liquid fuel preparation, in particular to a biomass green hydrogen poly-generation coupling system which comprises a transportation unit, a pretreatment unit, a gasification unit, a synthesis unit and a preparation unit which are sequentially connected. The raw materials sequentially pass through the transportation unit, the pretreatment unit, the gasification unit, the synthesis unit and the preparation unit to obtain the low-carbon-alcohol hydrogen storage liquid fuel, and the low-carbon-alcohol hydrogen storage liquid fuel is pumped into a collection room to be collected. Different products are produced in the process of preparing the low-carbon alcohol hydrogen storage liquid fuel from the raw materials, the biomass green hydrogen poly-generation coupling system is high in integration level, biomass such as low-quality agricultural and forestry waste is converted into high-quality green hydrogen, high-added-value green multi-carbon alcohol hydrogen storage liquid fuel and green methanol, and the biomass green hydrogen poly-generation coupling system has the advantages of being environmentally friendly, free of pollution and the like. And high-value conversion of energy and resource utilization of biomass is realized, so that the production cost of green hydrogen and hydrogen storage liquid fuel is reduced.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of low-carbon alcohol hydrogen storage liquid fuel preparation, and particularly relates to a biomass green hydrogen multi-cogeneration coupling system. BACKGROUND

[0002] The development and application of clean renewable energy can effectively alleviate energy crisis and environmental pollution. Hydrogen energy is a clean and environmentally friendly energy. Hydrogen can not only be used as a clean fuel for transportation and distributed heat and power generation, but more importantly, it can also be used as an energy storage medium for storing intermittent renewable resource-generated electricity, effectively solving the problem of abandoned wind and light. The key to whether hydrogen energy can be widely and efficiently utilized and large-scale industrialized is the lack of safe, low-cost, high-performance, and high-energy-density hydrogen storage technology.

[0003] Hydrogen storage and transportation is the key to whether hydrogen energy technology can be truly industrialized. In order to solve the bottleneck problems of hydrogen storage and transportation, researchers have developed various hydrogen storage technologies, such as compressed hydrogen, liquefied hydrogen, metal alloy, adsorption hydrogen storage, ammonia hydrogen storage, etc., but all have various problems. For example, the current naphthenic and nitrogen heterocyclic hydrogen storage liquid fuels are prepared from non-renewable fossil energy through a complex refining process, which not only increases the dependence of industrial production on petrochemical energy, but also causes a certain degree of pollution to the ecological environment. From the perspective of sustainable development and low carbon, it is urgent to explore a renewable green hydrogen production method. In the production of energy, fuel and chemicals, biomass such as agricultural and forestry waste is considered a promising and renewable fossil energy alternative green carbon source, with zero net carbon dioxide emissions. Based on this, the present application proposes a new idea of a biomass green hydrogen multi-cogeneration coupling system. SUMMARY

[0004] Therefore, the technical problem to be solved by the present application is how to produce green hydrogen from agricultural and forestry waste and co-produce multiple products, maintain the concept of low carbon, and achieve sustainable development.

[0005] The above technical problem is solved by the following technical scheme: the present application provides a biomass green hydrogen multi-cogeneration coupling system, which comprises a transportation unit, a pretreatment unit, a gasification unit, a synthesis unit and a preparation unit connected in sequence; and raw materials pass through the transportation unit, the pretreatment unit, the gasification unit, the synthesis unit and the preparation unit in sequence to obtain low-carbon alcohol hydrogen storage liquid fuel, which is pumped into a collection room for collection; and different products can be co-produced in the process of preparing low-carbon alcohol hydrogen storage liquid fuel from raw materials.

[0006] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the transportation unit comprises a raw material bin and a conveyor belt, and the raw material is transported from the raw material bin to the pretreatment unit through the conveyor belt for pretreatment.

[0007] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the pretreatment unit comprises primary treatment and secondary treatment, the primary treatment comprises drying, crushing, grinding and granulation of the raw material to obtain biomass solid shaped particles; and the secondary treatment comprises baking the obtained biomass solid shaped particles to obtain biochar.

[0008] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the biochar obtained by the pretreatment unit is pumped into the gasification unit, and the gasification unit comprises a gasification furnace, and the biochar is pyrolyzed and gasified in the gasification furnace to obtain green hydrogen synthesis gas.

[0009] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the green hydrogen synthesis gas is separated by pressure swing adsorption to obtain hydrogen for producing green hydrogen.

[0010] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the flue gas generated in the process of pyrolysis and gasification of the biochar in the gasification furnace is recycled back to the pretreatment unit to provide heat energy for the drying and baking processes of the pretreatment unit.

[0011] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the synthesis unit comprises a fixed bed reactor; and the green hydrogen synthesis gas obtained by the gasification unit is reacted with a CuCo-based catalyst in the fixed bed reactor to prepare a green low-carbon alcohol-water mixture.

[0012] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the preparation unit comprises a dehydration tower and a methanol rectification tower.

[0013] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the green low-carbon alcohol-water mixture is dehydrated by the dehydration tower, and the green low-carbon alcohol-water mixture is rectified by the methanol rectification tower to obtain methanol, and a low-carbon alcohol hydrogen storage liquid fuel is obtained.

[0014] In a preferred embodiment of the biomass green hydrogen poly-generation coupling system: the obtained low-carbon alcohol hydrogen storage liquid fuel is pumped into the collection room for collection.

[0015] The present application has the beneficial effect that: after the biomass raw material such as agricultural and forestry waste is treated by high-temperature pyrolysis gasification, hydrogen-rich synthesis gas can be prepared, and the hydrogen in the hydrogen-rich synthesis gas is extracted to prepare green hydrogen by using pressure swing adsorption technology. The hydrogen-rich synthesis gas after gasification of the biomass is prepared into a low-carbon alcohol water mixture in a fixed bed by catalytic pyrolysis, and then after water removal and demethanolization by a rectifying column, high-purity low-carbon alcohol hydrogen storage liquid fuel is obtained; the biomass green hydrogen poly-generation coupling system has high integration degree, can convert low-quality biomass such as agricultural and forestry waste into high-quality green hydrogen, high-value green low-carbon alcohol hydrogen storage liquid fuel and green methanol, realizes high-value conversion of energy and resources of the biomass, and further effectively reduces the production cost of green hydrogen and hydrogen storage liquid fuel. BRIEF DESCRIPTION OF DRAWINGS

[0016] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings of the embodiments of the present application will be briefly introduced below. Obviously, the drawings described below only relate to some embodiments of the present application, but not limit the present application. Among them: Figure 1 The overall structure schematic diagram of the biomass green hydrogen poly-generation coupling system is shown. DETAILED DESCRIPTION

[0017] In order to make those skilled in the art better understand the present application, the present application will be further described in detail below in combination with specific embodiments and drawings.

[0018] The terms used in the present application are those general terms currently widely used in the art in consideration of the functions about the present application, but these terms can be changed according to the intention of those skilled in the art, precedents or new technologies in the art. In addition, specific terms can be selected by the applicant, and in this case, the detailed meaning thereof will be described in the detailed description of the present application. Therefore, the terms used in the specification should not be understood as simple names, but based on the meaning of the terms and the overall description of the present application.

[0019] REFERENCE Figure 1The embodiment provides a biomass green hydrogen poly-generation coupling system, which comprises a transportation unit 1, a pretreatment unit 2, a gasification unit 3, a synthesis unit 4 and a preparation unit 5 connected in sequence; and raw materials pass through the transportation unit 1, the pretreatment unit 2, the gasification unit 3, the synthesis unit 4 and the preparation unit 5 in sequence to obtain low-carbon alcohol hydrogen storage liquid fuel, which is pumped into a collection room 6 for collection; and different products can be poly-generated from the process of preparing low-carbon alcohol hydrogen storage liquid fuel from raw materials, so that the resource utilization rate is further improved, the cost is reduced, the market competitiveness is enhanced, the environmental pollution is reduced and the resource recycling is realized, significant economic, technical and environmental benefits are achieved and the sustainable development concept is met; wherein, the raw materials used in the application mainly are biomass raw materials such as agricultural and forestry waste, the raw materials are transported to the pretreatment unit 2 through the transportation unit 1 for pretreatment, in the process, the raw materials can further generate various products such as biomass solid particles, through poly-generation, various components in the raw materials can be fully utilized and resource waste is reduced, then the products obtained after pretreatment are sequentially introduced into the gasification unit 3, the synthesis unit 4 and the preparation unit 5 for treatment, finally, low-carbon alcohol hydrogen storage liquid fuel can be obtained.

[0020] As an optional embodiment, the transportation unit 1 comprises a raw material bin 11 and a conveyor belt 12, the raw materials enter the pretreatment unit 2 for pretreatment through the conveyor belt 12 from the raw material bin 11.

[0021] As an optional embodiment, the pretreatment unit 2 is divided into multi-stage treatment, including primary treatment and secondary treatment, the primary treatment comprises a series of drying, crushing, grinding and granulation forming of the raw materials to obtain biomass solid shaped particles, specifically, hot air drying is carried out at 60-90 DEG C for 4-8h, crushing is carried out through a hammer crusher, the particle size is controlled to be less than 6mm, grinding is carried out through a ball mill for 20-50min, the particle size is generally 50-80 meshes, and 1cm shaped fuel is formed through an environmental granulator; the secondary treatment mainly comprises a low-temperature baking furnace, the biomass solid shaped particles obtained through the primary treatment are subjected to the low-temperature baking treatment through the low-temperature baking furnace, the low-temperature baking temperature is 220-260 DEG C, the original biomass particle heat value is 14-17MJ / kg, and the biochar particle heat value after the low-temperature baking is 18-23MJ / kg, so that the biochar with higher energy density can be obtained.

[0022] Wherein, when the raw materials are subjected to drying treatment, a rotary dryer, an air flow dryer and the like can be selected; when the raw materials are subjected to crushing treatment, a biomass crusher can be selected to crush through extrusion through a gear; when the raw materials are subjected to grinding treatment, a biomass grinder, a ball mill and the like can be selected; and when the raw materials are subjected to granulation forming treatment, a flat die granulator, a biomass granulator and the like can be selected.

[0023] It should be further noted that during this process, multiple different products can be co-produced; for example, biochar doped with nitrogen, phosphorus, and potassium can be used to produce biochar-based compound fertilizer. During the low-temperature baking pretreatment stage of biomass solid shaped particles, multiple products can also be co-produced, such as wood vinegar prepared by condensing gas during the low-temperature baking pretreatment of biomass, which can be used as raw material to further synthesize plant acid water-soluble fertilizer.

[0024] As an optional embodiment, the biochar obtained by the pretreatment unit 2 is pumped into the gasification unit 3, which includes a gasification furnace 31. The obtained biochar is pumped into the fixed bed or fluidized bed gasification furnace 31 for gasification to obtain green hydrogen synthesis gas. The hydrogen in the synthesis gas is separated by pressure swing adsorption technology, and the hydrogen is used to produce high-grade green hydrogen.

[0025] Specifically, after high-temperature gasification of biochar, hydrogen-rich synthesis gas can be obtained. By using pressure swing adsorption (PSA) technology to purify hydrogen from the hydrogen-rich synthesis gas, and by using gas chromatography and mass spectrometry to determine the purity of hydrogen, green hydrogen with a purity of up to 99.999% or even higher can be obtained, which is suitable for fuel cells, water electrolysis coupling processes, and high-purity gas application scenarios.

[0026] As an optional embodiment, the high-temperature flue gas generated during the pyrolysis and gasification of biochar in the gasification furnace 31 can be recycled back to the pretreatment unit 2 to provide heat energy for the drying and low-temperature baking of biomass, thereby improving the energy efficiency of the entire system.

[0027] The gasification furnace 31 is a device for pyrolysis and gasification of biochar, which includes a material inlet, a thermal decomposition zone, a reduction-oxidation zone, a reaction product zone, a catalyst region, a water vapor injection port, a water discharge pipe, a gas outlet, and a heat insulation layer. Biochar enters the furnace from the material inlet and begins to decompose in the thermal decomposition zone under high temperature, generating gaseous products such as hydrogen and methane, as well as solid products such as carbon black. Subsequently, these gaseous products enter the reduction-oxidation zone, where they are further converted into more useful gases such as hydrogen and methane through reaction with water vapor. Finally, the reaction products are collected in the reaction product zone and discharged through the gas outlet. Throughout the process, water vapor is injected from the top to participate in the reaction and help the gasification of biochar.

[0028] As an optional embodiment, the synthesis unit 4 includes a fixed bed reactor 41. After reforming and adjusting the obtained synthesis gas, it is subjected to gasification and synthesis reaction in the fixed bed reactor 41 under the action of CuCo-based catalyst to prepare green low-carbon alcohol-water mixture.

[0029] The fixed bed reactor 41 provides an opportunity for reactants to fully contact the catalyst when a continuous flow of gas or liquid passes through a stationary solid catalyst bed, thereby promoting the progress of chemical reactions, which is commonly used in the preparation of green low-carbon alcohol in gasification and synthesis reactions.

[0030] It should be further pointed out that reforming modification is a process for regulating the composition ratio of synthesis gas (H2 and CO), aiming to optimize its composition by changing the hydrogen carbon ratio (H2 / CO), removing impurity gases (such as CO2, CH4) or introducing modifiers (such as water vapor, CO2) to meet the thermodynamic and kinetic requirements of subsequent catalytic synthesis reactions. This process plays an important role in improving the conversion rate, yield and selectivity of green low-carbon alcohol (such as methanol, ethanol or mixed alcohol) synthesis reactions, especially in the process of using raw synthesis gas generated by biomass gasification or solid waste pyrolysis, the composition is usually deviated from the optimal zone of catalytic reaction, so it is necessary to realize component matching and process efficient coupling through reforming modification, here mainly using water gas shift, CO2 dry reforming and steam reforming reactions to cooperatively regulate the hydrogen / carbon ratio.

[0031] As an optional embodiment, the preparation unit 5 is composed of a dehydration tower and a methanol rectification tower. The rectification tower double-tower system can utilize the boiling point difference of different components to effectively separate and purify the water and methanol components in the mixture. Further, the prepared green low-carbon alcohol-water mixture is purified and separated by the rectification tower (double-tower) process; the dehydration tower removes the water in the mixture system, and the methanol rectification tower rectifies the methanol from the low-carbon alcohol system to obtain high-purity low-carbon alcohol hydrogen storage liquid fuel, which is pumped into the collection room 6 for collection.

[0032] In summary, through the full-chain flexible coupling system, multi-cogeneration of high-value products can be realized, obtaining high-purity green hydrogen and green methanol, green low-carbon alcohol (hydrogen storage liquid fuel) while cogenerating biomass solid formed particles, biochar, biochar-based compound fertilizer, wood vinegar, plant acid water-soluble fertilizer and other high-quality products. At the same time, the proposed process can effectively solve the problems of green hydrogen preparation and purification. The purity of methanol and low-carbon alcohol is determined by gas chromatography, and the purity of green methanol is as high as 99%, and the purity of green low-carbon alcohol is as high as 97%.

[0033] Referring to Figure 1 and Table 1, the present embodiment provides an experimental method based on a biomass green hydrogen multi-cogeneration coupling system, through a double-tower low-carbon mixed alcohol precise separation process and technology, the water content of the dehydration tower inlet end and receiving end, the methanol purity of the methanol rectification tower receiving tank, the C2 + alcohol purity data of each group experiment are obtained.

[0034] Specifically, the low-carbon mixed alcohol-water mixture is directly pumped into the lower column section of the dehydration tower after passing through the first preheating furnace (preheating device before the dehydration tower), and the gas-liquid balance in the dehydration tower is optimized through a three-stage precise temperature control system. The steam distilled from the top of the dehydration tower is condensed into a liquid by the shell-and-tube condenser to the reflux tank on the dehydration tower, and a low-carbon alcohol mixed solution containing a very small amount of water is obtained in the dehydration tower receiving tank by adjusting the reflux ratio; in the dehydration tower, the jacket temperature of the first column bottom (the kettle-type heating area at the bottom of the dehydration tower) is 120-160°C, the bottom temperature is controlled at 77-85°C, the temperature in the column is 70-76°C, the top temperature is 64-69°C, the rectification time is 12-24h, the reflux ratio is 1:1, and the reflux pump power is 25-85%.

[0035] Further, the receiving tank of the dehydration tower is the feed tank of the methanol rectification tower. The liquid in the methanol rectification tower feed tank is pumped into the middle column section of the demethanizing tower through the second preheating furnace (preheating device before the methanol rectification tower), the gas-liquid balance in the demethanizing tower is optimized through a three-stage precise temperature control system, the steam distilled from the top of the methanol rectification tower is condensed to the reflux tank on the methanol rectification tower, and a low-carbon alcohol with a purity of >95% is obtained in the methanol rectification tower receiving tank by adjusting the reflux ratio. In the demethanizing tower, the jacket temperature of the second column bottom (the kettle-type heating area at the bottom of the methanol rectification tower) is 150-170°C, the bottom temperature is controlled at 76-91°C, the temperature in the column is 69-75°C, the top temperature is 65-68°C, the rectification time is 12-24h, the reflux ratio is 1:1, and the reflux pump power is 25-85%.

[0036] Table 1 Analysis of products in each stage of each group of experiments

[0037] The detailed operation of experiment 1 through the double-tower low-carbon mixed alcohol precise separation process and technology is as follows: ①The low-carbon mixed alcohol-water mixture prepared from synthesis gas is subjected to Agilent liquid chromatography analysis to obtain the content of each component, and the low-carbon mixed alcohol-water mixture is prepared according to the above proportions, wherein the water is 74.88kg, the methanol is 23.88kg, the ethanol is 16.00kg, the n-propanol is 6.00kg, the n-butanol is 1.80kg, the n-pentanol is 0.68kg, and the n-hexanol is 0.28kg.

[0038]

[0039]

[0040] Experiment 2: The detailed operation of the double-tower low-carbon mixed alcohol precise separation process and technology is as follows:

[0041]

[0042] ​​​​③The receiving tank of the dehydration tower (the feed tank of the methanol rectification tower) is pumped into the middle tower section of the methanol rectification tower through the second preheating furnace, the temperature of the second preheating furnace is 175℃, the second tower pot jacket temperature is 158℃, the lower tower temperature of the methanol rectification tower is 88℃, the middle tower temperature is 73℃, the upper tower temperature is 67℃, the rectification time is 21h, the upper-middle-lower three-section precise temperature control is adopted, the gas-liquid components in the demethanolization tower are finely adjusted, most of the methanol in the mixed liquid is removed, and then the reflux is used to achieve deep methanol removal, the reflux ratio is 1:1, the reflux pump power is 60%, high-purity methanol is obtained in the receiving tank of the methanol rectification tower, and high-purity C2+alcohol is obtained at the bottom of the tank, and the components are analyzed by Agilent liquid chromatography as shown in Table 1.

[0043] The detailed operation of experiment 3 through the double-tower low-carbon mixed alcohol precise separation process and technology is as follows: ①The low-carbon mixed alcohol-water mixture prepared from synthesis gas is analyzed by Agilent liquid chromatography to obtain the content of each component, and the low-carbon mixed alcohol-water mixture is prepared according to the above-mentioned proportion, wherein the water is 74.23kg, the methanol is 22.94kg, the ethanol is 15.79kg, the n-propanol is 5.83kg, the n-butanol is 1.75kg, the n-pentanol is 0.64kg, and the n-hexanol is 0.26kg.

[0044] ②The above-mentioned low-carbon mixed alcohol-water mixture is placed in the feed tank of the dehydration tower, and is pumped into the lower tower section of the dehydration tower through the first preheating furnace, the temperature of the first preheating furnace is 135℃, the first tower pot jacket temperature is 140℃, the lower tower temperature of the dehydration tower is 78℃, the middle tower temperature is 75℃, and the upper tower temperature is 68℃, the rectification time is 19h, the upper-middle-lower three-section precise temperature control is adopted, the gas-liquid components in the water removal tower are finely adjusted, most of the waste water in the mixed liquid is removed, and then the reflux is used to achieve deep water removal, the reflux ratio is 1:1, the reflux pump power is 70%, and the liquid components obtained in the receiving tank of the dehydration tower are analyzed by Agilent liquid chromatography as shown in Table 1.

[0045] ③The receiving tank of the dehydration tower (the feed tank of the methanol rectification tower) is pumped into the middle tower section of the methanol rectification tower through the second preheating furnace, the temperature of the second preheating furnace is 177℃, the second tower pot jacket temperature is 168℃, the lower tower temperature of the methanol rectification tower is 88℃, the middle tower temperature is 72℃, the upper tower temperature is 67℃, the rectification time is 18h, the upper-middle-lower three-section precise temperature control is adopted, the gas-liquid components in the demethanolization tower are finely adjusted, most of the methanol in the mixed liquid is removed, and then the reflux is used to achieve deep methanol removal, the reflux ratio is 1:1, the reflux pump power is 60%, high-purity methanol is obtained in the receiving tank of the methanol rectification tower, and high-purity C2+alcohol is obtained at the bottom of the tank, and the components are analyzed by Agilent liquid chromatography as shown in Table 1.

[0046] The detailed operation of experiment 4 through the double-tower low-carbon mixed alcohol precise separation process and technology is as follows: The low-carbon mixed alcohol-water mixture prepared from synthesis gas is subjected to Agilent liquid chromatography analysis to obtain the content of each component, and the low-carbon mixed alcohol-water mixture is prepared according to the above proportions, wherein the water is 75.03 kg, the methanol is 22.98 kg, the ethanol is 16.04 kg, the n-propanol is 6.08 kg, the n-butanol is 1.79 kg, the n-pentanol is 0.69 kg, and the n-hexanol is 0.33 kg.

[0047] The low-carbon mixed alcohol-water mixture is placed in the feed tank of the dehydration tower, and is pumped into the lower tower section of the dehydration tower through the first preheating furnace, the temperature of the first preheating furnace is 138°C, the temperature of the first tower pot jacket is 145°C, the temperature of the lower tower section of the dehydration tower is 82°C, the temperature of the middle tower section is 72°C, the temperature of the upper tower section is 65°C, the rectification time is 23h, the gas-liquid components in the dehydration tower are finely adjusted through the upper-middle-lower three-section precise temperature control, and most of the waste water in the mixed liquid is removed, and then deep dehydration is achieved through reflux, the reflux ratio is 1:1, the reflux pump power is 55%, and the receiving tank of the dehydration tower obtains the liquid components which are subjected to Agilent liquid chromatography analysis, as shown in Table 1.

[0048] The receiving tank of the dehydration tower (the feed tank of the methanol rectification tower) is pumped into the middle tower section of the methanol rectification tower through the second preheating furnace, the temperature of the second preheating furnace is 160°C, the temperature of the second tower pot jacket is 155°C, the temperature of the lower tower section of the methanol rectification tower is 87°C, the temperature of the middle tower section is 72°C, the temperature of the upper tower section is 67°C, the rectification time is 21h, the gas-liquid components in the methanol rectification tower are finely adjusted through the upper-middle-lower three-section precise temperature control, most of the methanol in the mixed liquid is removed, and then deep methanol removal is achieved through reflux, the reflux ratio is 1:1, the reflux pump power is 65%, the receiving tank of the methanol rectification tower obtains high-purity methanol, and the bottom of the tank obtains high-purity C2+ alcohol, and the components are subjected to Agilent liquid chromatography analysis, as shown in Table 1.

[0049] The detailed operation of the double-tower low-carbon mixed alcohol precise separation process and technology is as follows: The low-carbon mixed alcohol-water mixture prepared from synthesis gas is subjected to Agilent liquid chromatography analysis to obtain the content of each component, and the low-carbon mixed alcohol-water mixture is prepared according to the above proportions, wherein the water is 75.03 kg, the methanol is 22.98 kg, the ethanol is 16.04 kg, the n-propanol is 6.08 kg, the n-butanol is 1.79 kg, the n-pentanol is 0.69 kg, and the n-hexanol is 0.33 kg.

[0050] The low-carbon mixed alcohol-water mixture is placed in the feed tank of the dehydration tower, and is pumped into the lower tower section of the dehydration tower through the first preheating furnace. The temperature of the first preheating furnace is 138°C, and the temperature of the first tower pot jacket is 142°C. The temperature of the lower tower section of the dehydration tower is 83°C, the temperature of the middle tower section is 75°C, and the temperature of the upper tower section is 68°C. The rectification time is 16h. Through the three-section precise temperature control, the gas-liquid components in the dehydration tower are finely adjusted, and most of the waste water in the mixed liquid is removed. Deep dehydration is achieved through reflux. The reflux ratio is 1:1, and the reflux pump power is 45%. The receiving tank of the dehydration tower obtains the liquid component, which is analyzed by Agilent liquid chromatography, as shown in Table 1.

[0051] The receiving tank of the dehydration tower (the feed tank of the methanol rectification tower) is pumped into the middle tower section of the methanol rectification tower through the second preheating furnace. The temperature of the second preheating furnace is 165°C, and the temperature of the second tower pot jacket is 159°C. The temperature of the lower tower section of the methanol rectification tower is 89°C, the temperature of the middle tower section is 72°C, and the temperature of the upper tower section is 67°C. The rectification time is 23h. Through the three-section precise temperature control, the gas-liquid components in the methanol rectification tower are finely adjusted, and most of the methanol in the mixed liquid is removed. Deep methanol removal is achieved through reflux. The reflux ratio is 1:1, and the reflux pump power is 58%. The receiving tank of the methanol rectification tower obtains high-purity methanol, and the pot bottom obtains high-purity C2+alcohol. The components are analyzed by Agilent liquid chromatography, as shown in Table 1.

[0052] Finally, it should be noted that the methods and apparatuses described in detail above are only embodiments, and those skilled in the art can modify these embodiments in different ways without departing from the scope of the present application.

Claims

1. A biomass green hydrogen cogeneration coupling system, characterized in that: The biomass green hydrogen cogeneration coupling system comprises, in sequence, a transport unit (1), a pretreatment unit (2), a gasification unit (3), a synthesis unit (4), and a preparation unit (5); and, The raw materials pass through the transportation unit (1), pretreatment unit (2), gasification unit (3), synthesis unit (4) and preparation unit (5) in sequence to obtain low-carbon alcohol hydrogen storage liquid fuel, which is then pumped into the collection room (6) for collection; and different products can be produced in the process of preparing low-carbon alcohol hydrogen storage liquid fuel from the raw materials.

2. The biomass green hydrogen cogeneration coupling system according to claim 1, characterized in that: The transport unit (1) includes a raw material silo (11) and a conveyor belt (12). The raw material enters the pretreatment unit (2) from the raw material silo (11) via the conveyor belt (12) for pretreatment.

3. The biomass green hydrogen cogeneration coupling system according to claim 2, characterized in that: The pretreatment unit (2) includes primary treatment and secondary treatment. The primary treatment includes drying, crushing, grinding and granulating the raw materials to obtain biomass solid pellets. The secondary processing includes baking the obtained biomass solid pellets to obtain biochar.

4. The biomass green hydrogen cogeneration coupling system according to claim 3, characterized in that: The biochar obtained by the pretreatment unit (2) is pumped into the gasification unit (3), which includes a gasifier (31). The biochar is pyrolyzed and gasified by the gasifier (31) to obtain green hydrogen synthesis gas.

5. The biomass green hydrogen cogeneration coupling system according to claim 4, characterized in that: The green hydrogen synthesis gas is produced by separating hydrogen through pressure swing adsorption (PSA) to produce green hydrogen.

6. The biomass green hydrogen cogeneration coupling system according to claim 4 or 5, characterized in that: The gasifier (31) recycles the flue gas generated during the biochar pyrolysis and gasification process back to the pretreatment unit (2), providing heat energy for the drying and baking process of the pretreatment unit (2).

7. The biomass green hydrogen cogeneration coupling system according to claim 4, characterized in that: The synthesis unit (4) includes a fixed-bed reactor (41). A green low-carbon alcohol-water mixture is prepared by reacting the green hydrogen syngas obtained from the gasification unit (3) with a CuCo-based catalyst in the fixed-bed reactor (41).

8. The biomass green hydrogen cogeneration coupling system according to claim 7, characterized in that: The preparation unit (5) consists of a dehydration tower and a methanol distillation tower.

9. The biomass green hydrogen cogeneration coupling system according to claim 8, characterized in that: The water in the green low-carbon alcohol-water mixture is removed by a dehydration tower, and methanol is distilled from the green low-carbon alcohol-water mixture by a methanol distillation tower to obtain low-carbon alcohol hydrogen storage liquid fuel.

10. The biomass green hydrogen cogeneration coupling system according to claim 9, characterized in that: The obtained low-carbon alcohol hydrogen storage liquid fuel is pumped into the collection chamber (6) for collection.

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