System and method for preparing methanol by dynamically coupling organic solid waste gasification and green hydrogen

Abstract

This invention relates to the field of new energy and resource recycling technology. It provides a system and method for the dynamic coupling of organic solid waste gasification and green hydrogen to produce methanol. Through multi-module collaboration and energy coupling, it achieves a deep integration of solid waste resource utilization with renewable energy hydrogen production and carbon recycling. The organic solid waste hydrothermal carbonization module, wind / solar power generation module, water electrolysis hydrogen production module, and methanol synthesis reaction module are integrated into a single unit. A hydrothermal carbonization and liquid-phase byproduct co-gasification technology is employed, dynamically controlling the CO and CO2 yields under the action of a catalyst. Online monitoring using a mass spectrometer regulates reaction conditions, ensuring stable syngas composition and meeting the optimal H2 / CO ratio required for methanol synthesis. The photovoltaic and wind power systems, through hybrid energy storage and power prediction algorithms, adjust the operating power of the water electrolysis unit in real time, automatically matching the hydrogen yield with the gasification rate to ensure the continuous and stable methanol synthesis reaction.

Description

Technical Field

[0001] This invention relates to the field of new energy and resource recycling technology, specifically a system and method for the dynamic coupling of organic solid waste gasification and green hydrogen to prepare methanol. Background Technology

[0002] With the continued growth of global energy demand and the increasing depletion of fossil fuel resources, developing clean and renewable energy alternatives has become a crucial issue in the energy sector. Methanol, as an important chemical raw material and clean fuel, has broad application prospects in energy storage, transportation, and chemical synthesis. Traditional methanol production primarily uses fossil fuels as raw materials, consuming non-renewable resources and generating greenhouse gas emissions during the process. Meanwhile, the treatment and disposal of organic solid waste such as municipal solid waste, agricultural waste, and sludge has become a significant issue in environmental protection. Achieving clean treatment and resource utilization of organic solid waste is a research direction in waste management. On the other hand, renewable energy sources such as photovoltaic and wind power are clean and low-carbon, but their power generation processes are intermittent and fluctuating, affecting the stable utilization of renewable energy.

[0003] To address the challenges of resource utilization of organic solid waste and renewable energy consumption, existing technologies have attempted to couple the gasification products of organic solid waste with hydrogen produced from water electrolysis using renewable energy sources for methanol synthesis. Current coupling systems typically control the gasification and hydrogen production processes separately according to preset operating conditions, lacking a closed-loop dynamic coordination mechanism based on feedback from the syngas composition. When the composition of the organic solid waste, the composition of the gasification products, or the power output of wind and solar power generation change, it becomes difficult to match the syngas composition at the gasification end with the hydrogen supply at the hydrogen production end in a timely manner, causing the H2 / CO ratio to deviate from the range required for methanol synthesis. Summary of the Invention

[0004] To address the shortcomings of existing technologies, the purpose of this invention is to provide a system and method for the dynamic coupling of organic solid waste gasification and green hydrogen production to prepare methanol. The technical problem to be solved by this invention is: how to solve the problem of difficulty in matching the composition of syngas and the amount of hydrogen supply when the raw materials and wind and solar power fluctuate through closed-loop coordinated control of the gasification end and the hydrogen production end.

[0005] It achieves multi-dimensional integrated coupling of carbon, hydrogen, and energy, improving system energy efficiency and resource utilization; the hydrothermal carbonization is mild and can treat solid waste with high water content, avoiding energy consumption in the pre-drying process; it efficiently converts and utilizes renewable energy, alleviating power fluctuation problems; the product is clean and has high added value, realizing a closed loop of conversion from waste to green methanol; it has modular and intelligent control features, and is suitable for distributed energy systems and carbon neutrality engineering applications.

[0006] To solve the above-mentioned technical problems, the first inventive solution provided by the present invention is: a system for the dynamic coupling of organic solid waste gasification and green hydrogen to produce methanol, including a solid waste treatment module, a water electrolysis hydrogen production module, a methanol gasification reaction module and a wind / solar power generation module; The solid waste treatment module includes a hydrothermal reactor and a three-phase separator. The hydrothermal reactor is connected to the three-phase separator through a pipeline. The organic solid waste raw material is subjected to subcritical hydrothermal treatment in the hydrothermal reactor to form a three-phase product including hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas. The three-phase separator is connected to the methanol gasification reaction module through three-phase product conveying pipelines. The separated hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas are sent to the methanol gasification reaction module through the corresponding three-phase product conveying pipelines. Each three-phase product conveying pipeline is equipped with an electrically controlled valve. The water electrolysis hydrogen production module includes a water electrolysis device and a dynamic controller. The hydrogen outlet of the water electrolysis device is connected to the methanol gasification reaction module through a hydrogen delivery pipeline. An electrically controlled valve is installed on the hydrogen delivery pipeline, and the dynamic controller is connected to the water electrolysis device. The methanol gasification reaction module is equipped with a gasification reaction heater, a catalyst bed, a catalyst bed heater, and a mass spectrometer for monitoring the volume fraction of CO, CO2, and H2 gases. The methanol gasification reaction module is also connected to a steam delivery pipeline, which is equipped with an electrically controlled valve. The wind and solar power generation modules are electrically connected to the dynamic controller to power the water electrolysis equipment. The control unit is connected to each of the aforementioned electrically controlled valves, the gasification reaction heater, the catalyst bed heater, the mass spectrometer, and the dynamic controller. The control unit is used to determine the actual H2 / CO value based on the H2 gas volume fraction and CO gas volume fraction monitored by the mass spectrometer, compare the actual H2 / CO value with the preset H2 / CO target range, and adjust the opening degree of the electrically controlled valves, the temperature of the gasification reaction heater, and the temperature of the catalyst bed heater on each three-phase product delivery pipeline, steam delivery pipeline, and hydrogen delivery pipeline according to the comparison result. It also outputs an operating power adjustment command to the dynamic controller. The dynamic controller adjusts the operating power of the water electrolysis equipment according to the output power of the wind / solar power generation module and the operating power adjustment command to coordinate and adjust the syngas composition at the gasification end and the hydrogen supply at the hydrogen production end.

[0007] After one adjustment, the mass spectrometer re-monitors the volume fractions of H2 and CO gases, and the control unit cyclically executes the comparison and adjustment process based on the updated actual H2 / CO value. When the actual H2 / CO value is lower than the target range, the control unit increases the operating power of the water electrolysis equipment and increases the opening of the electrically controlled valve on the hydrogen delivery pipeline; when the actual H2 / CO value is higher than the target range, the control unit decreases the operating power of the water electrolysis equipment and decreases the opening of the electrically controlled valve. The coordinated adjustment between the gasification end and the hydrogen production end reduces the supply and demand deviation caused by fluctuations in the composition of organic solid waste, the composition of gas produced by gasification, and the power of wind and solar power generation, thus maintaining the actual H2 / CO value within the preset target range.

[0008] Preferably, each pipeline between the three-phase separator and the methanol gasification reaction module for conveying the hydrothermal liquid, hydrothermal charcoal, and hydrothermal reaction gas is equipped with a hydrothermal liquid tank, a hydrothermal charcoal tank, and a syngas tank. The hydrothermal liquid tank, hydrothermal charcoal tank, and syngas tank can effectively mitigate fluctuations in the output of the solid waste treatment module. Furthermore, the hydrothermal charcoal tank allows for precise adjustment of the hydrothermal charcoal supply through valve opening, thereby enabling real-time control of the steam / carbon ratio in conjunction with the steam delivery volume.

[0009] Preferably, the product outlet of the methanol gasification reaction module is connected to the inlet of a three-way valve via a main pipeline, the first outlet of the three-way valve is connected to a distillation purification device and a methanol storage tank via a pipeline, and the second outlet of the three-way valve is connected to a reaction gas storage tank, a separation and purification device and a synthesis gas tank via a pipeline.

[0010] When the H2 / CO ratio deviates from the target range, directly introducing the gasification products into the methanol synthesis unit will lead to a decrease in methanol yield or catalyst poisoning. This solution uses a three-way valve to guide the substandard reaction gas into a reaction gas storage tank and a separation and purification unit. After separation and purification, it is then sent to the synthesis gas tank, where it can serve as supplementary feedstock for the gasification reaction or as a source for further gasification / blending. The substandard synthesis gas will not directly enter the methanol storage tank but will be recycled back to the front end of the system to participate in the reaction again, avoiding material waste and product defects.

[0011] Preferably, the system further includes a first waste heat recovery device, which is connected to the methanol gasification reaction module and the hydrothermal reactor via pipelines. The oxygen outlet of the water electrolysis equipment is connected to the first waste heat recovery device via an oxygen delivery pipeline. This not only significantly reduces the need for external heating sources but also utilizes oxygen to assist combustion or participate in oxidation reactions to release heat, achieving high-value utilization of byproducts and indirectly mitigating the impact of wind and solar power fluctuations on the overall system operation.

[0012] Preferably, the water electrolysis equipment is one of an alkaline electrolyzer, a proton exchange membrane electrolyzer, or a solid oxide electrolyzer. A hydrogen tank is installed on the hydrogen delivery pipeline between the water electrolysis equipment and the methanol gasification reaction module, and an oxygen tank is installed on the oxygen delivery pipeline between the water electrolysis equipment and the first waste heat recovery device. Electrically controlled valves connected to the controller are installed on the hydrogen delivery pipeline, the oxygen delivery pipeline, and the pipeline connecting the first waste heat recovery device and the thermal reactor.

[0013] Preferably, the system also includes a second waste heat recovery device, which is connected to the three-phase separator and the hydrothermal reactor via pipelines to reduce the system's external energy consumption.

[0014] This invention also provides a method for the dynamic coupling of organic solid waste gasification and green hydrogen to prepare methanol, comprising the following steps: The organic solid waste raw material is subjected to subcritical hydrothermal treatment to obtain a three-phase product including hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas. The three-phase product is then separated into three phases, and the separated hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas are respectively sent to the methanol gasification reaction module. Hydrogen is produced by water electrolysis using an electrolysis water device. The generated hydrogen is then sent to the methanol gasification reaction module via a hydrogen delivery pipeline, where the hydrogen reacts with the hydrothermal carbon, hydrothermal liquid, and hydrothermal reaction gas to produce methanol. A target H2 / CO range is set in the control unit. The volume fractions of CO, CO2, and H2 gases in the methanol gasification reaction module are monitored using a mass spectrometer. The control unit determines the actual H2 / CO value based on the monitored H2 and CO gas volume fractions and compares the actual H2 / CO value with the target H2 / CO range. When the actual H2 / CO value deviates from the target H2 / CO range, the control unit adjusts the gasification reaction temperature, steam / carbon ratio, and catalyst bed temperature of the methanol gasification reaction module according to the comparison results. The control unit determines the target operating power of the water electrolysis equipment based on the comparison results and outputs an operating power adjustment command to the dynamic controller. The dynamic controller adjusts the operating power of the water electrolysis equipment according to the output power of the wind / solar power generation module and the operating power adjustment command. The control unit synchronously adjusts the opening of the electrically controlled valve on the hydrogen delivery pipeline and cyclically executes the comparison and adjustment process based on the updated actual H2 / CO value until the actual H2 / CO value is within the target H2 / CO range.

[0015] Preferably, the target H2 / CO range is 2.0 to 2.2. When the actual H2 / CO value is lower than the lower limit of the target H2 / CO range, the control unit determines the first current density setting value, the first power setting value, and the first opening setting value of the electrically controlled valve on the hydrogen delivery pipeline based on the first deviation between the actual H2 / CO value and the lower limit value, and controls the dynamic controller and the electrically controlled valve to operate according to the corresponding first setting value. When the actual H2 / CO value is higher than the upper limit of the target H2 / CO range, the control unit determines the second current density setting value, the second power setting value, and the second opening setting value of the electrically controlled valve on the hydrogen delivery pipeline based on the second deviation between the actual H2 / CO value and the upper limit value, and controls the dynamic controller and the electrically controlled valve to operate according to the corresponding second setting value. When the actual H2 / CO value is within the target H2 / CO range, the control unit uses the current current density setting value, the current power setting value, and the current opening setting value as the setting value for the next control cycle.

[0016] Preferably, the control unit adopts a multivariable closed-loop coordinated control algorithm, which adjusts the gasification reaction temperature, steam / carbon ratio, catalyst bed temperature, operating power of water electrolysis equipment and hydrogen delivery flow rate according to the deviation of the actual H2 / CO value from the target range of H2 / CO, as well as the actual measured values ​​of CO gas volume fraction, CO2 gas volume fraction, gasification reaction temperature, catalyst bed temperature and output power of wind / solar power generation module.

[0017] Compared with the prior art, the beneficial effects of the present invention are: This invention first performs subcritical hydrothermal treatment on organic solid waste raw materials, then separates and separately transports the resulting hydrothermal char, hydrothermal liquid, and hydrothermal reaction gas into three phases. The hydrothermal liquid is an aqueous product with water as the continuous phase and containing organic carbonaceous components and inorganic components. The hydrothermal reaction gas contains carbonaceous gases and reactive gases generated during the hydrothermal treatment. The hydrothermal char, hydrothermal liquid, and hydrothermal reaction gas are respectively fed into a methanol gasification reaction module to participate in the gasification, reforming, and methanol preparation reactions, thus utilizing the carbon source in the three-phase products. The separate transportation of the three-phase products also provides a structural basis for the independent adjustment of the feed rate of each phase. The flow rate of the hydrothermal reaction gas can be used as an adjustment variable for the composition of the syngas at the gasification end. The volume fractions of CO, CO2, and H2 gases in the methanol gasification reaction module are monitored using a mass spectrometer. The controller determines the actual H2 / CO value based on the volume fractions of H2 and CO gases and compares the actual H2 / CO value with a preset target range. When the actual H2 / CO ratio deviates, the control unit adjusts the three-phase product delivery rate, steam delivery rate, gasification reaction temperature, and catalyst bed temperature to change the composition of the syngas at the gasification end. It also determines the target operating power of the water electrolysis unit based on the comparison of the actual H2 / CO ratio and outputs an operating power adjustment command to the dynamic controller. The dynamic controller, in conjunction with the output power of the wind / solar power generation module, adjusts the current density and operating power of the water electrolysis unit to change the hydrogen production rate; the control unit synchronously adjusts the opening of the electrically controlled valves on the hydrogen delivery pipeline to change the hydrogen delivery flow rate to the methanol gasification reaction module. The operating power of the water electrolysis unit is used to regulate the continuous hydrogen production, and the electrically controlled valves on the hydrogen delivery pipeline are used to regulate the instantaneous hydrogen flow rate; together with the reaction conditions at the gasification end, they form a closed-loop coordinated control system.

[0018] This invention also includes a methanol purification and storage branch and a reaction gas separation and reflux branch. The product output from the methanol gasification reaction module is sent to the methanol storage tank after distillation and purification, while the reaction gas is sent back to the synthesis gas tank after separation and purification, thus realizing the recovery and utilization of unreacted gases. The first and second waste heat recovery devices form heat recovery paths between the methanol gasification reaction module, the three-phase separator, and the hydrothermal reactor, respectively, reducing the external heating demand of the hydrothermal treatment process. Attached Figure Description

[0019] Figure 1 This is a system diagram of the synthesis of methanol from organic solid waste and water produced by photovoltaic / wind power electrolysis according to the present invention.

[0020] Figure 2 This is a flowchart of the closed-loop control process for the H2 / CO ratio of the present invention.

[0021] Figure 3 This is a schematic diagram of the multivariate coordinated control relationship of the present invention.

[0022] Explanation of reference numerals in the attached figures: 1. Organic solid waste raw material; 2. Hydrothermal reactor; 3. Three-phase separator; 4. Hydrothermal liquid tank; 5. Hydrothermal carbon tank; 6. Syngas tank; 7. Methanol synthesis reaction module; 8. First waste heat recovery device; 9. Oxygen tank; 10. Hydrogen tank; 11. Water electrolysis equipment; 12. Dynamic controller; 13. Wind / solar power generation module; 14. Methanol storage tank; 15. Distillation and purification device; 16. Reaction gas storage tank; 17. Separation and purification device; 18. Second waste heat recovery device. Detailed Implementation

[0023] To make the above-mentioned objectives, features, and advantages of the embodiments of this application more apparent and understandable, the technical solutions of the embodiments of this application will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of this application, and not all of them. All other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0024] The following is for reference. Figure 1 A system diagram illustrating the dynamic coupling of organic solid waste gasification and green hydrogen to prepare methanol according to an embodiment of the present invention is provided.

[0025] like Figure 1 As shown, a system for producing methanol by dynamic coupling of organic solid waste gasification and green hydrogen includes a solid waste treatment module, a water electrolysis hydrogen production module, a methanol gasification reaction module 7, and a wind / solar power generation module 13.

[0026] The solid waste treatment module includes a hydrothermal reactor 2 and a three-phase separator 3. The hydrothermal reactor 2 is connected to the three-phase separator 3 via pipelines. The organic solid waste raw material 1 undergoes subcritical hydrothermal treatment in the hydrothermal reactor 2 to form a three-phase product including hydrothermal char, hydrothermal liquid, and hydrothermal reaction gas. The three-phase separator 3 is connected to the methanol gasification reaction module 7 via three-phase product conveying pipelines. The separated hydrothermal char, hydrothermal liquid, and hydrothermal reaction gas are respectively sent to the methanol gasification reaction module 7 via corresponding three-phase product conveying pipelines. Hydrothermal liquid tank 4, hydrothermal char tank 5, and synthesis gas tank 6 are respectively installed on the pipelines between the three-phase separator 3 and the methanol gasification reaction module 7 for conveying hydrothermal liquid, hydrothermal char, and hydrothermal reaction gas. The product outlet of the methanol gasification reaction module 7 is connected to the inlet of the three-way valve through the main pipeline. The first outlet of the three-way valve is connected to the distillation and purification device 15 and the methanol storage tank 14 in sequence through the pipeline. The second outlet of the three-way valve is connected to the reaction gas storage tank 16, the separation and purification device 17 and the synthesis gas tank 6 in sequence through the pipeline.

[0027] The water electrolysis hydrogen production module includes a water electrolysis device 11 and a dynamic controller 12. The hydrogen outlet of the water electrolysis device 11 is connected to the methanol gasification reaction module 7 via a hydrogen delivery pipeline. An electrically controlled valve is installed on the hydrogen delivery pipeline. The dynamic controller 12 is connected to the water electrolysis device 11. The water electrolysis device 11 is one of an alkaline electrolyzer, a proton exchange membrane electrolyzer, or a solid oxide electrolyzer. A hydrogen tank 10 is installed on the hydrogen delivery pipeline between the water electrolysis device 11 and the methanol gasification reaction module 7, and an oxygen tank 9 is installed on the oxygen delivery pipeline between the water electrolysis device 11 and the first waste heat recovery device 8.

[0028] The methanol gasification reaction module 7 is equipped with a gasification reaction heater, a catalyst bed, a catalyst bed heater, and a mass spectrometer for monitoring the volume fraction of CO and H2 gases. The methanol gasification reaction module 7 is also connected to a steam delivery pipeline, which is equipped with an electrically controlled valve. Each of the three-phase product delivery pipelines is also equipped with an electrically controlled valve.

[0029] The wind / solar power generation module 13 is connected to the dynamic controller 12. The system also includes a control unit, which is connected to each electrically controlled valve, the gasification reaction heater, the catalyst bed heater, the mass spectrometer, and the dynamic controller 12. The control unit is used to determine the actual H2 / CO value based on the H2 gas volume fraction and CO gas volume fraction monitored by the mass spectrometer, compare the actual H2 / CO value with the preset H2 / CO target range, and adjust the opening degree of the electrically controlled valves, the temperature of the gasification reaction heater, and the temperature of the catalyst bed heater on each three-phase product conveying pipeline, steam conveying pipeline, and hydrogen conveying pipeline according to the comparison result. It also outputs an operating power adjustment command to the dynamic controller 12. The dynamic controller 12 adjusts the operating power of the water electrolysis equipment 11 according to the output power of the wind / solar power generation module 13 and the operating power adjustment command to coordinate and adjust the syngas composition at the gasification end and the hydrogen supply at the hydrogen production end. The system also includes a first waste heat recovery device 8, which is connected to the methanol gasification reaction module 7 and the hydrothermal reactor 2 via pipelines. The oxygen outlet of the water electrolysis equipment 11 is connected to the first waste heat recovery device 8 via an oxygen delivery pipeline. The system also includes a second waste heat recovery device 18, which is connected to the three-phase separator 3 and the hydrothermal reactor 2 via pipelines.

[0030] A method for preparing methanol by dynamic coupling of organic solid waste gasification and green hydrogen includes: S1. The organic solid waste raw material 1 is subjected to subcritical hydrothermal treatment to obtain a three-phase product including hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas. The three-phase product is separated into three phases, and the separated hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas are respectively sent to methanol gasification reaction module 7.

[0031] S2. Hydrogen is produced by water electrolysis using water electrolysis equipment 11. The generated hydrogen is sent to methanol gasification reaction module 7 through hydrogen delivery pipeline, so that the hydrogen reacts with hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas to produce methanol.

[0032] S3. Set the H2 / CO target range in the controller. Use a mass spectrometer to monitor the volume fractions of CO, CO2, and H2 gases in the methanol gasification reaction module 7. The control unit determines the actual H2 / CO value based on the monitored H2 and CO gas volume fractions and compares the actual H2 / CO value with the H2 / CO target range. The H2 / CO target range is 2.0 to 2.2. When the actual H2 / CO value is lower than the lower limit of the H2 / CO target range, the control unit determines the first current density setting value, the first power setting value, and the first opening setting value of the electrically controlled valve on the hydrogen delivery pipeline of the water electrolysis equipment 11 based on the first deviation between the actual H2 / CO value and the lower limit value, and controls the dynamic controller 12 and the electrically controlled valve to operate according to the corresponding first setting values. When the actual H2 / CO value is higher than the upper limit of the target H2 / CO range, the control unit determines the second current density setting value, the second power setting value, and the second opening setting value of the electrically controlled valve on the hydrogen delivery pipeline of the water electrolysis equipment 11 based on the second deviation between the actual H2 / CO value and the upper limit value, and controls the dynamic controller 12 and the electrically controlled valve to operate according to the corresponding second setting values. When the actual H2 / CO value is within the target H2 / CO range, the control unit uses the current current density setting value, the current power setting value, and the current opening setting value as the setting values ​​for the next control cycle. When the actual H2 / CO value deviates from the target range, the control unit adjusts the gasification reaction temperature, steam / carbon ratio, and catalyst bed temperature of the methanol gasification reaction module 7 according to the comparison results. The control unit determines the target operating power of the water electrolysis equipment 11 according to the comparison results and outputs an operating power adjustment command to the dynamic controller 12. The dynamic controller 12 adjusts the operating power of the water electrolysis equipment 11 according to the output power of the wind / solar power generation module 13 and the operating power adjustment command. The control unit synchronously adjusts the opening of the electrically controlled valve on the hydrogen delivery pipeline and cyclically executes the comparison and adjustment process according to the updated actual H2 / CO value until the actual H2 / CO value is within the target range. The controller employs a multivariable closed-loop coordinated control algorithm. Based on the deviation of the actual H2 / CO value from the target range of H2 / CO, the volume fraction of CO gas, the volume fraction of CO2 gas, the gasification reaction temperature, the catalyst bed temperature, and the output power of the wind / solar power generation module 13, it determines the adjustment amounts of the gasification reaction temperature, steam / carbon ratio, catalyst bed temperature, operating power of the water electrolysis equipment 11, and hydrogen delivery flow rate. Based on each adjustment amount, it adjusts the gasification reaction temperature, steam / carbon ratio, catalyst bed temperature, operating power of the water electrolysis equipment 11, and hydrogen delivery flow rate respectively.

[0033] The hydrothermal liquid tank, hydrothermal carbon tank, and syngas tank temporarily store the hydrothermal liquid, hydrothermal carbon, and hydrothermal reaction gas, respectively. This buffers fluctuations between the output of the three-phase separator and the feed rate of the methanol gasification reaction module, and supports separate metering and adjustment of the three-phase products. The syngas tank is also used to collect the hydrothermal reaction gas and the separated and purified reflux gas, stabilizing the gas supply pressure and flow rate of the gaseous feedstock.

[0034] The three-way valve is used to switch between the methanol product processing path and the reaction gas recovery path. The methanol-containing product enters the methanol storage tank after distillation and purification, while the unreacted gas is temporarily stored, separated and purified, and then returned to the synthesis gas tank. H2, CO and CO2 can be recovered from it, reducing the loss of carbon source and hydrogen, and reducing the disturbance of the reflux gas to the operating status of the methanol gasification reaction module.

[0035] The oxygen produced by the water electrolysis unit is fed into the first waste heat recovery device, where it can serve as an oxidizing or combustion-supporting medium. This allows the combustible exhaust gas to oxidize and release heat within the device, and the resulting heat is then supplied to the hydrothermal reactor after heat exchange. This design utilizes the oxygen produced as a byproduct of water electrolysis and the system's combustible gas to provide heat for hydrothermal treatment, reducing the need for external heating.

[0036] A hydrogen tank is installed on the hydrogen output pipeline to buffer hydrogen flow fluctuations caused by changes in wind and solar power generation and downstream hydrogen consumption. A pressure sensor monitors the supply pressure of the pipeline and hydrogen tank, providing signals for overpressure protection and low-pressure alarms. A flow meter detects the actual hydrogen delivery volume, enabling the controller to adjust the operating power and valve opening of the water electrolysis equipment based on the actual H2 / CO ratio and hydrogen flow rate.

[0037] The three-phase products discharged from the three-phase separator still carry the heat generated by the hydrothermal reaction. The second waste heat recovery device can recover the heat from the hydrothermal liquid, hydrothermal carbon, hydrothermal reaction gas, and flash steam, and use the recovered heat to preheat the feed of the hydrothermal reactor. This design can also reduce the temperature of the three-phase products before they enter the storage tank, reducing the thermal shock of high-temperature materials to the storage tank and conveying components.

[0038] Example 2 like Figure 2 As shown, this embodiment is used to verify the effect of the linkage adjustment between the gasification end and the electrolysis hydrogen production end on the stability of the H2 / CO ratio when the composition of organic solid waste changes.

[0039] 1. System configuration and testing conditions The calculation is performed using a combination of material balance and control procedures.

[0040] Hydrothermal reactor 2 is a continuous stirred reactor with an effective volume of 75L, and three-phase separator 3 has an effective volume of 120L. The effective volumes of hydrothermal liquid tank 4, hydrothermal carbon tank 5, and syngas tank 6 are 0.60m³, 0.25m³, and 0.80m³, respectively. Hydrogen tank 10 has an effective volume of 0.60m³ and an allowable operating pressure of 1.20MPa-1.80MPa. The hydrogen delivery pipeline is equipped with a pressure sensor with a range of 0MPa-2.50MPa and a flow meter with a range of 0Nm³ / h-10.0Nm³ / h. Unless otherwise specified, all pressures are absolute pressures.

[0041] The standard gas volume was based on 0℃ and 101.325 kPa, and the gas composition was expressed as the volume fraction on a dry basis after water removal. The mass spectrometer was configured with two sampling positions: the first sampling position was located after the gasification product had been purified and pressurized, but before hydrogen injection; the second sampling position was located after the hydrogen injection port, but before the methanol synthesis catalyst bed. The mass spectrometer acquired data every 5 seconds, and the controller performed a coordination adjustment every 30 seconds.

[0042] The methanol gasification reaction module 7, along the material flow direction, includes a gasification zone, a dust removal zone, a cooling and purification zone, a pressurization zone, a hydrogen mixing zone, and a methanol synthesis zone. The gasified product sequentially passes through a cyclone separator, a ceramic filter with a filtration accuracy of 5μm, and zinc oxide desulfurization material, resulting in a hydrogen sulfide concentration of no more than 0.1 mg / Nm³ after purification. The purified gas is then pressurized to 5.0 MPa by a compressor and mixed with hydrogen obtained from water electrolysis.

[0043] The methanol synthesis zone is packed with 15L of copper-zinc-aluminum catalyst, with an inlet temperature of 235℃ and a gas hourly space velocity (GHSV) of 2600 h⁻¹. -1 .

[0044] 2. Calculation of control parameters The actual H2 / CO value detected at the second sampling location is calculated according to formula (1): In the formula, This represents the actual H2 / CO ratio. and These are the dry basis volume fractions of H2 and CO detected at the second sampling location, respectively.

[0045] H2 / CO target value Take 2.10, and set the allowable range to 2.0-2.2. The hydrogen flow rate required to supplement the water electrolysis equipment 11 is calculated according to formula (2):

[0046] In the formula, The target flow rate for hydrogen electrolysis is expressed in Nm³ / h. This represents the gasification production flow rate at the first sampling location, in Nm³ / h. and These are the dry basis volume fractions of CO and H2 in the gasification products, respectively.

[0047] After considering the pressure deviation of hydrogen tank 10, the target hydrogen production flow rate is calculated according to formula (3): In the formula, The target hydrogen production flow rate is expressed in Nm³ / h. The pressure compensation coefficient is taken as 3.0 Nm³ / (h·MPa). The target pressure for hydrogen tank 10 is set at 1.50 MPa. The pressure of hydrogen tank 10 is measured by a pressure sensor, in MPa. A result below 0 is taken as 0, and a result above 8.0 Nm³ / h is taken as 8.0 Nm³ / h.

[0048] The water electrolysis equipment 11 uses an alkaline electrolysis cell stack composed of 40 effective electrolysis units connected in series. The effective area of ​​a single electrolysis unit is 1500 cm², and the Faraday efficiency is 0.96. The target current is calculated according to formula (4):

[0049] In the formula, The target current for the electrolytic cell is expressed in amperes (A). The value is Faraday's constant, taken as 96485 C / mol. For Faraday efficiency, The number of effective electrolysis units, The molar volume of the gas at 0℃ and 101.325 kPa is taken as 0.022414 Nm³ / mol, and 3600 is the conversion factor between hours and seconds.

[0050] The target current density is calculated according to equation (5): In the formula, The target current density is expressed in A / cm². This represents the effective area of ​​a single electrolysis unit, expressed in cm².

[0051] The target operating power of the water electrolysis equipment 11 is calculated according to formula (6): In the formula, Target operating power, in kW. This refers to the cell stack voltage, measured in volts (V). The auxiliary power for the circulating pump, cooling unit, and gas-liquid separation unit is taken as 1.2kW, and 1000 is the conversion factor between W and kW.

[0052] The electrically controlled valves on the hydrogen delivery pipeline are controlled by incremental PI control. The hydrogen flow deviation is calculated according to formula (7):

[0053] The opening degree of the electrically controlled valve is updated according to formula (8): In the formula, This represents the hydrogen flow rate deviation at the k-th sampling time, in Nm³ / h. The flow rate of hydrogen gas detected by the flow meter is expressed in Nm³ / h. For the opening degree of the electrically controlled valve, Take 4.0% / (Nm³ / h), Take 0.08% / [Nm³ / (h·s)], Take 5 seconds. Valve opening is limited to 10%-90%.

[0054] The steam / carbon ratio is calculated according to formula (9): In the formula, The molar flow rate of water carried by the hydrothermal fluid. For the added steam molar flow rate, , and These represent the molar flow rates of carbon in hydrothermal carbon, hydrothermal liquid, and hydrothermal reaction gas, respectively, with each molar flow rate measured in mol / h.

[0055] When the actual H2 / CO ratio is below 2.0, the controller increases the electrolytic hydrogen flow rate and gradually increases the gasification reaction temperature and steam / carbon ratio based on offline calibration results. When the actual H2 / CO ratio is above 2.2, the opposite adjustment is performed. The adjustment amount for the gasification reaction temperature in a single control cycle shall not exceed 4℃, and the adjustment amount for the steam / carbon ratio in a single control cycle shall not exceed 0.04.

[0056] Catalyst bed temperature is not used as a direct correction variable for H2 / CO. When the total feed flow rate or gas composition changes, the catalyst bed temperature is adjusted within the range of 230℃-240℃ to maintain the reaction load in the methanol synthesis zone.

[0057] 3. Subcritical hydrothermal treatment Kitchen waste organic matter and dewatered sludge were mixed at a dry basis mass ratio of 7:3. The moisture content of the mixed raw materials was 68.4%, and the dry basis carbon mass fraction was 46.1%. Organic solid waste raw material 1 was fed into hydrothermal reactor 2 at a rate of 100 kg / h and continuously processed at 220℃ and 2.50 MPa, with an average residence time of 45 min.

[0058] After separation by three-phase separator 3, the hydrothermal products yielded 15.2 kg / h of hydrothermal carbon, 78.0 kg / h of hydrothermal liquid, and 3.1 Nm³ / h of hydrothermal reaction gas. The carbon mass fraction of the hydrothermal carbon was 72.0%, the total carbon concentration of the hydrothermal liquid was 25.0 g / kg, and the water mass fraction was 97.5%. The volume fractions of CO2, CO, H2, and N2 in the hydrothermal reaction gas were 64.0%, 14.0%, 8.0%, and 14.0%, respectively.

[0059] The carbon flow rate of the raw material is 14.57 kg / h, the total carbon flow rate of the three-phase products is 14.19 kg / h, and the carbon balance closure rate is 97.4%.

[0060] 18.0 kg / h of the hydrothermal fluid is fed into methanol gasification reaction module 7, and the remaining 60.0 kg / h is returned to the raw material preparation stage. All hydrothermal char and hydrothermal reaction gas are fed into methanol gasification reaction module 7.

[0061] 4. Initial Run The pressure in the gasification zone is 0.35 MPa, and the gasification reaction temperature is 760℃. The applied steam flow rate is 4.3 kg / h, and based on the amount of water carried by the hydrothermal fluid, the steam / carbon ratio is 1.15.

[0062] The purified gasification product flow rate was 35.0 Nm³ / h. At the first sampling location, the volume fraction of H₂ was detected to be 38.0%, the volume fraction of CO was 25.0%, and the volume fraction of CO₂ was 18.0%. The H₂ flow rate in the gasification product was 13.30 Nm³ / h, and the CO flow rate was 8.75 Nm³ / h.

[0063] According to equation (2), the target flow rate for hydrogen electrolysis is: According to equation (4), the target current of the electrolytic cell is: According to equation (5), the target current density is: The voltage of the electrolytic cell stack is 80.0V. According to equation (6), the operating power of the water electrolysis equipment 11 is: The hydrogen delivery valve was open at 43%, and the pressure in hydrogen tank 10 was 1.50 MPa. The actual H2 / CO ratio measured at the second sampling location was 2.10.

[0064] 5. Disturbance in raw material composition After the system has been running stably for 30 minutes, the dry weight ratio of kitchen waste organic matter to dewatered sludge is adjusted to 5:5. The adjusted raw material has a moisture content of 74.2% and a dry weight carbon content of 42.8%.

[0065] Ninety seconds after the feedstock switch, the purified gasification gas flow rate became 34.0 Nm³ / h. At the first sampling location, the volume fraction of H₂ was detected to be 36.0%, the volume fraction of CO was 26.0%, and the volume fraction of CO₂ was 20.5%. The H₂ flow rate in the gasification gas was 12.24 Nm³ / h, and the CO flow rate was 8.84 Nm³ / h.

[0066] Before the hydrogen flow rate adjustment was completed, the actual H2 / CO ratio detected at the second sampling location dropped to 1.96. Based on equation (2), the target flow rate for hydrogen electrolysis was recalculated as follows:

[0067] The controller adjusts the opening of the hydrogen delivery valve from 43% to 56%. The dynamic controller 12 adjusts the electrolysis current from 316A to 393A, the current density from 0.211A / cm² to 0.262A / cm², and the operating power from 26.5kW to 32.6kW.

[0068] The gasification reaction temperature was adjusted from 760℃ to 768℃ over two control cycles, and the steam / carbon ratio was adjusted from 1.15 to 1.23. The catalyst bed temperature was adjusted from 235℃ to 237℃ to accommodate changes in the mixed gas flow rate. The three-phase product delivery rate remained constant.

[0069] 6. Dynamic adjustment results After adjustment for 180 seconds, the purified gasification gas production flow rate was 34.3 Nm³ / h. The volume fraction of H2 detected at the first sampling location was 39.2%, the volume fraction of CO was 25.1%, and the volume fraction of CO2 was 18.2%.

[0070] According to equation (2), the target flow rate for hydrogen electrolysis is: The dynamic controller 12 adjusts the electrolytic cell current to 288A and the operating power to 24.2kW. The actual H2 / CO value detected at the second sampling position recovers to 2.03 at 90s, reaches 2.08 at 180s, and then remains between 2.05 and 2.13 for 10 minutes.

[0071] Under control conditions, the gasification reaction temperature was maintained at 760℃, the steam / carbon ratio at 1.15, the catalyst bed temperature at 235℃, the electrolytic hydrogen flow rate at 5.08 Nm³ / h, and the hydrogen valve opening at 43%. Under the same feedstock disturbance, the actual H₂ / CO ratio remained between 1.94 and 1.99 within 15 minutes.

[0072] After the dry basis composition and moisture content of the raw materials changed, the closed-loop coordinated control enabled the actual H2 / CO value to recover to 2.0-2.2 within 180s and remain stable during subsequent operation. The fixed parameter control condition failed to recover to the target range.

[0073] Calculation results show that coordinated adjustment of gasification reaction conditions, electrolysis hydrogen production, and hydrogen transport flow rate can reduce the deviation in syngas ratio caused by raw material fluctuations.

[0074] Example 3 like Figure 3 As shown, this embodiment is used to verify the effects of power prediction, hydrogen buffering, and gasification end compensation on the stability of methanol synthesis feedstock and system heat utilization when wind and solar power generation power decreases.

[0075] 1. Initial operating conditions The system structure, gas standard state, mass spectrometer sampling location, and controller sampling cycle are the same as in Example 2.

[0076] The organic solid waste treatment capacity is 100 kg / h, the hydrothermal reaction temperature is 220℃, the reaction pressure is 2.50 MPa, and the average residence time is 45 min. The gasification reaction temperature is 760℃, the steam / carbon ratio is 1.15, and the catalyst bed temperature is 235℃.

[0077] The initial output power of the wind / solar power generation module 13 is 38.0 kW. The operating power of the water electrolysis device 11 is 26.5 kW, and the hydrogen electrolysis flow rate is 5.08 Nm³ / h. The pressure of the hydrogen tank 10 is 1.50 MPa, and the actual H2 / CO ratio detected at the second sampling location is 2.10.

[0078] 2. Wind and solar power prediction The output power of wind / solar power generation module 13 is sampled every 30 seconds. The predicted power for the next control cycle is calculated according to equation (10):

[0079] In the formula, This represents the current wind and solar power output, in kW. The predicted power for the next control cycle, in kW, with a smoothing coefficient. Take 0.60.

[0080] The electrolysis power executed by the dynamic controller 12 is determined according to equation (11): In the formula, The power output of the water electrolysis equipment 11 is expressed in kW. The target operating power is calculated using equation (6), in kW.

[0081] 3. Decrease in wind and solar power output After the system has been running for 20 minutes, the output power of the wind / solar power generation module 13 has decreased from 38.0kW to 20.0kW. According to equation (10), the predicted power for the next control cycle is 24.5kW, and the dynamic controller 12 first limits the operating power of the water electrolysis device 11 to 24.5kW.

[0082] The wind and solar power output then remained at 20.0kW-21.0kW, the operating power of the water electrolysis equipment 11 decreased to 20.5kW, and the electrolysis hydrogen flow rate decreased to 3.90Nm³ / h.

[0083] The hydrogen tank 10 releases stored hydrogen, maintaining the hydrogen delivery flow rate at 4.80 Nm³ / h-5.05 Nm³ / h for the first 8 minutes after the power reduction. The gas temperature inside the hydrogen tank 10 is calculated at 25°C, and the pressure decreases from 1.50 MPa to 1.47 MPa.

[0084] The standard volume of hydrogen corresponding to the pressure drop is calculated according to formula (12): In the formula, The standard volume of hydrogen gas released is expressed in Nm³. The effective volume of the hydrogen tank is 10, taken as 0.60 m³. and These are the absolute pressures before and after the pressure drop, in kPa. The standard pressure is taken as 101.325 kPa. The standard temperature is 273.15 K. The temperature of the gas inside hydrogen tank 10 is taken as 298.15K.

[0085] Substituting the data, we get: The cumulative hydrogen shortage within 8 minutes is 0.14 Nm³, which is less than the amount released from hydrogen tank 10.

[0086] 4. Gasification end compensation When the operating power of the water electrolysis unit 11 is limited, the controller adjusts the gasification reaction temperature from 760℃ to 768℃ and the steam / carbon ratio from 1.15 to 1.25. The catalyst bed temperature is adjusted from 235℃ to 237℃ to adapt to changes in the gasification composition and feed load.

[0087] After parameter adjustment, the gasification gas flow rate detected at the first sampling location was 34.2 Nm³ / h, with an H₂ volume fraction of 40.8%, a CO volume fraction of 24.0%, and a CO₂ volume fraction of 17.5%. The H₂ flow rate in the gasification gas was 13.95 Nm³ / h, and the CO flow rate was 8.21 Nm³ / h.

[0088] According to equation (2), the target flow rate for hydrogen electrolysis is: The water electrolysis unit 11 provides 3.90 Nm³ / h of hydrogen at an operating power of 20.5 kW. The controller adjusts the opening of the hydrogen delivery valve from 43% to 38%, and the hydrogen flow rate into the hydrogen mixing zone is 3.29 Nm³ / h, with the remaining hydrogen entering the hydrogen tank 10.

[0089] The lowest actual H2 / CO value detected at the second sampling location was 1.98. After deviating from the target range for 30 seconds, it recovered to 2.04 and remained between 2.04 and 2.14 during low-power operation.

[0090] 5. Wind and solar power output power recovery After 10 minutes of low power operation, the output power of the wind / solar power generation module 13 recovered to 36.0 kW. The dynamic controller 12 restored the operating power of the water electrolysis equipment 11 to 26.5 kW and the electrolytic hydrogen flow rate to 5.08 Nm³ / h.

[0091] The pressure in hydrogen tank 10 recovered to 1.50 MPa within 6 minutes. The gasification reaction temperature, steam / carbon ratio, and catalyst bed temperature recovered to 760℃, 1.15, and 235℃, respectively. During power recovery, the actual H2 / CO ratio remained between 2.06 and 2.16.

[0092] 6. Product splitting and reaction gas recovery When the actual H2 / CO ratio is below 2.0 for 30 consecutive seconds, the three-way valve switches to the branch where the reaction gas storage tank 16 is located. The reaction gas is cooled by the inlet cooling section, and the condensate is discharged from the bottom of the reaction gas storage tank 16. The gas phase is returned to the synthesis gas tank 6 after the separation and purification device 17 removes moisture and impurities.

[0093] After the actual H2 / CO ratio enters the 2.0-2.2 range and remains there for 120 seconds, the three-way valve switches to the branch where the distillation purification unit 15 is located. The distillation purification unit 15 completes product condensation, gas-liquid separation, and methanol purification, and the purified liquid is sent to the methanol storage tank 14.

[0094] The calculation results after 6 hours of continuous operation are as follows: the flow rate of the reaction gas entering the reaction gas storage tank 16 is 4.5 Nm³ / h, and the flow rate of the gas returning to the synthesis gas tank 6 after separation and purification is 3.4 Nm³ / h.

[0095] 7. First waste heat recovery The first waste heat recovery device 8 includes an oxidation chamber and a heat exchanger. Oxygen generated by the water electrolysis equipment 11 is buffered by an oxygen tank 9 and then sent into the oxidation chamber.

[0096] During the stable operation phase, the oxygen flow rate generated by the water electrolysis equipment 11 is 2.54 Nm³ / h, the actual oxygen supply flow rate of the oxidation chamber is 1.0 Nm³ / h, and the remaining oxygen is output through the external supply pipeline after being stabilized by the oxygen tank 9.

[0097] The flow rate of combustible exhaust gas entering the oxidation chamber is 4.5 Nm³ / h, of which the volume fraction of H2 is 18.0% and the volume fraction of CO is 22.0%. The recovered heat power of the first waste heat recovery device 8 is calculated according to formula (13):

[0098] In the formula, The recovered heat power of the first waste heat recovery device 8 is expressed in kW. For heat exchange efficiency, we take 0.72. The standard volumetric flow rate of combustible exhaust gas is expressed in Nm³ / h. Take 0.022414 Nm³ / mol, and These are the dry basis volume fractions of H2 and CO in the exhaust gas, respectively. Take 241.8 kJ / mol, Take 283.0 kJ / mol.

[0099] Substituting the data, the theoretical heat release power is: The heat recovery power of the first waste heat recovery device 8 is: 8. Secondary waste heat recovery The hydrothermal liquid, hydrothermal carbon, and hydrothermal reaction gas discharged from the three-phase separator 3 enter the hot side of the second waste heat recovery device 18. The average temperature of the three-phase products before entering the heat exchanger is 172°C, and the average temperature after leaving the heat exchanger is 82°C.

[0100] The feed for hydrothermal reactor 2 is the cold-side material, with a feed flow rate of 100 kg / h, an average specific heat of 3.8 kJ / (kg·℃), and the feed temperature is increased from 25℃ to 70℃.

[0101] The recovered heat power of the second waste heat recovery device 18 is calculated according to formula (14): In the formula, The recovered heat power of the second waste heat recovery device 18 is expressed in kW. The feed flow rate for hydrothermal reactor 2 is expressed in kg / h. This represents the average specific heat of the feed, expressed in kJ / (kg·℃). and These are the feed temperatures before and after preheating, respectively, in °C.

[0102] Substituting the data, we get: When the two-stage waste heat recovery devices are running together, the external heating power of the hydrothermal reactor 2 is reduced from 24.8kW to 15.9kW.

[0103] 9. Comparison Results By shutting down the wind and solar power prediction and gasification end coordination adjustment under the operating conditions, the operating power of the water electrolysis equipment 11 was reduced only according to the real-time output power of the wind and solar power. After the wind and solar power output power dropped to 20.0kW, the actual H2 / CO ratio was as low as 1.82, and remained below 2.0 for 9.5 minutes.

[0104] After adopting wind and solar power prediction, hydrogen tank 10 buffer and gasification end coordinated adjustment, the actual H2 / CO value was as low as 1.98, and the time of deviation from the target range was 30s.

[0105] When the wind and solar power output decreased from 38.0kW to 20.0kW, the coordinated control increased the minimum H2 / CO ratio from 1.82 in the control condition to 1.98, and shortened the time of deviation from the target range from 9.5min to 30s. The total recovered heat power obtained by the two-stage waste heat recovery device was 8.95kW, which reduced the external heating power of hydrothermal reactor 2 by 35.9%.

[0106] Calculation results show that the system can mitigate hydrogen supply deviations caused by renewable energy fluctuations and reduce external heating requirements for the hydrothermal treatment process.

[0107] Obviously, those skilled in the art can make various modifications and variations to this invention without departing from its spirit and scope. Therefore, if these modifications and variations fall within the scope of the claims of this invention and their equivalents, this invention also intends to include these modifications and variations.

Claims

1. A system for preparing methanol by dynamically coupling organic solid waste gasification and green hydrogen, characterized in that, include: The system includes a solid waste treatment module, a water electrolysis hydrogen production module, a methanol gasification reaction module (7), and a wind and solar power generation module (13). The solid waste treatment module includes a hydrothermal reactor (2) and a three-phase separator (3). The three-phase separator (3) is connected to the methanol gasification reaction module (7) through three-phase product conveying pipelines, and each three-phase product conveying pipeline is equipped with an electrically controlled valve. The methanol gasification reaction module (7) is equipped with a gasification reaction heater, a catalyst bed, a catalyst bed heater, and a mass spectrometer for monitoring the volume fraction of CO, CO2, and H2 gases. The chemical reaction module (7) is also connected to a steam transmission pipeline, which is equipped with an electrically controlled valve. The water electrolysis hydrogen production module includes an electrolysis water device (11) and a dynamic controller (12). The hydrogen outlet of the electrolysis water device (11) is connected to the methanol gasification reaction module (7) through a hydrogen transmission pipeline. The dynamic controller (12) is connected to the electrolysis water device (11) and is used to adjust the operating power of the electrolysis water device (11). An electrically controlled valve is installed on the hydrogen transmission pipeline. The wind and solar power generation module (13) is electrically connected to the dynamic controller (12) and is used to supply power to the electrolysis water device. The control unit is connected to the electrically controlled valves of each delivery pipeline, the gasification reaction heater, the catalyst bed heater, the mass spectrometer, and the dynamic controller. Based on the H2 and CO volume fractions fed back by the mass spectrometer, it calculates the actual H2 / CO value and compares it with its preset target range. Accordingly, it adjusts the valve opening of the three-phase product delivery pipeline, the steam delivery pipeline, and the hydrogen delivery pipeline, the temperature of the gasification reaction heater, and the heating temperature of the catalyst bed heater. At the same time, it sends a power adjustment signal to the dynamic controller. The dynamic controller coordinates the adjustment of the operating power of the water electrolysis equipment based on the real-time output power of the wind and solar power generation module and the power adjustment signal to achieve dynamic matching between the syngas composition at the gasification end and the hydrogen supply at the hydrogen production end.

2. The system for producing methanol by dynamic coupling of organic solid waste gasification and green hydrogen according to claim 1, characterized in that, The target range for H2 / CO is 2.0 to 2.

2.

3. The system for producing methanol by dynamic coupling of organic solid waste gasification and green hydrogen according to claim 1, characterized in that, The control unit adopts a multivariable closed-loop coordinated control algorithm. Based on the deviation of the actual H2 / CO value from the target range of H2 / CO, as well as the actual measured values ​​of CO gas volume fraction, CO2 gas volume fraction, gasification reaction temperature, catalyst bed temperature, and output power of the wind / solar power generation module (13), the control unit adjusts the gasification reaction temperature, steam / carbon ratio, catalyst bed temperature, operating power of the water electrolysis equipment (11), and hydrogen delivery flow rate.

4. The system for preparing methanol by dynamic coupling of organic solid waste gasification and green hydrogen according to claim 1, characterized in that, The three-phase separator (3) and the methanol gasification reaction module (7) are connected by a hydrothermal liquid tank (4), a hydrothermal carbon tank (5), and a synthesis gas tank (6) on the pipelines used to transport hydrothermal liquid, hydrothermal carbon, and hydrothermal reaction gas.

5. The system for producing methanol by dynamic coupling of organic solid waste gasification and green hydrogen according to claim 4, characterized in that, The product outlet of the methanol gasification reaction module (7) is connected to the inlet of the three-way valve through the main pipeline. The first outlet of the three-way valve is connected to the distillation and purification device (15) and the methanol storage tank (14) in sequence through the pipeline. The second outlet of the three-way valve is connected to the reaction gas storage tank (16), the separation and purification device (17) and the synthesis gas tank (6) in sequence through the pipeline.

6. The system for dynamically coupling organic solid waste gasification and green hydrogen to produce methanol according to claim 1, characterized in that, It also includes a first waste heat recovery device (8), which is connected to the methanol gasification reaction module (7) and the hydrothermal reactor (2) through pipelines respectively. The oxygen outlet of the water electrolysis equipment (11) is connected to the first waste heat recovery device (8) through an oxygen delivery pipeline.

7. The system for the dynamic coupling of organic solid waste gasification and green hydrogen to produce methanol according to claim 6, characterized in that, The water electrolysis equipment (11) is one of an alkaline electrolysis cell, a proton exchange membrane electrolysis cell, or a solid oxide electrolysis cell. A hydrogen tank (10) is installed on the hydrogen delivery pipeline between the water electrolysis equipment (11) and the methanol gasification reaction module (7). An oxygen tank (9) is installed on the oxygen delivery pipeline between the water electrolysis equipment (11) and the first waste heat recovery device (8). The hydrogen delivery pipeline, the oxygen delivery pipeline, and the pipeline connecting the first waste heat recovery device (8) and the thermal reactor (2) are all equipped with electrically controlled valves connected to the control unit.

8. The system for producing methanol by dynamic coupling of organic solid waste gasification and green hydrogen according to claim 1, characterized in that, It also includes a second waste heat recovery device (18), which is connected to the three-phase separator (3) and the hydrothermal reactor (2) respectively through pipelines.

9. The preparation method used in the methanol preparation system of organic solid waste gasification and green hydrogen dynamic coupling according to claim 1, characterized in that, Includes the following steps: Organic solid waste raw material (1) is fed into hydrothermal reactor (2) for subcritical hydrothermal treatment to obtain three-phase products including hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas. The obtained three-phase products are separated into three phases, and the separated hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas are respectively sent into methanol gasification reaction module (7). Hydrogen is produced by water electrolysis using an electrolysis water device (11). The generated hydrogen is sent to the methanol gasification reaction module (7) through a hydrogen transmission pipeline, so that the hydrogen reacts with hydrothermal carbon, hydrothermal liquid and hydrothermal reaction gas to produce methanol. The H2 / CO target range is set in the control unit. The volume fractions of CO, CO2 and H2 gas in the methanol gasification reaction module (7) are monitored by a mass spectrometer. The control unit determines the actual H2 / CO value based on the monitored H2 gas volume fraction and CO gas volume fraction, and compares the actual H2 / CO value with the H2 / CO target range. When the actual H2 / CO value deviates from the H2 / CO target range, the control unit adjusts the gasification reaction temperature, steam / carbon ratio and catalyst bed temperature of the methanol gasification reaction module (7) according to the comparison results. The control unit determines the target operating power of the water electrolysis equipment (11) according to the comparison results and outputs the operating power adjustment command to the dynamic controller (12). The dynamic controller (12) adjusts the operating power of the water electrolysis equipment (11) according to the output power of the wind / solar power generation module (13) and the operating power adjustment command. The controller synchronously adjusts the opening of the electrically controlled valve on the hydrogen delivery pipeline and cyclically executes the comparison and adjustment process according to the updated actual H2 / CO value until the actual H2 / CO value is within the H2 / CO target range.

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