Green energy conversion and utilization method and system

Abstract

This invention discloses a method and system for green energy conversion and utilization, comprising the following steps: A storage and transportation system analyzes the collected biomass / organic matter on-site, and pre-treats the biomass / organic matter according to the analysis results to obtain at least one of compressed pellets, pyrolysis char, and pyrolysis oil; a green energy conversion and storage system generates electricity using green energy, while simultaneously feeding the pre-treated compressed pellets and pyrolysis char from the storage and transportation system into a gasification unit for gasification. The generated pyrolysis gas undergoes a synthesis reaction with hydrogen produced from water electrolysis to obtain green synthetic fuel; the green energy conversion and storage system then reacts the pre-treated pyrolysis oil from the storage and transportation system with hydrogen produced from water electrolysis under high temperature and pressure to undergo a hydrogenation and deoxygenation upgrading reaction to obtain green refined oil. This invention can increase the carbon content and energy density per unit volume of biomass / organic matter, reduce transportation costs, and economically provide a carbon source for large-scale conversion of green electricity into green synthetic fuel and green refined oil.

Description

Technical Field

[0001] This invention relates to the field of green energy conversion and utilization technology, and in particular to a green energy conversion and utilization method and system. Background Technology

[0002] Deep-sea energy islands utilize the deep sea (water depth > 50 meters, offshore > 30 kilometers) as their carrier. Currently, there are two main technological approaches for deep-sea energy islands. The first approach fully utilizes various renewable energy sources in the area where the floating deep-sea energy island is located, such as wind, solar, and wave energy, to generate electricity. Hydrogen produced by water electrolysis is then combined with carbon dioxide from the exhaust of combustion energy sources (gas turbines or diesel engines, etc.) to synthesize green synthetic fuels. Alternatively, air carbon capture can be combined with the hydrogen produced by water electrolysis on the deep-sea energy island to synthesize green synthetic fuels, forming a zero-emission, energy-self-sufficient system. The second approach attempts to convert and transmit various renewable energy sources such as wind, solar, and wave energy in the area where the deep-sea energy island is located back to land. For example, renewable energy can be converted into electricity and transmitted directly back to land via submarine cables, or liquid hydrogen produced by water electrolysis can be transported back to land.

[0003] The first technological route for producing green synthetic fuels relies solely on carbon dioxide from exhaust gases from the combustion of fuels on deep-sea energy islands and from the atmosphere. This approach is limited in quantity and cost, making large-scale and economical implementation impossible, limiting it to self-sufficiency. The second technological route faces challenges due to the fact that deep-sea energy islands are typically over 100 kilometers from land. Long-distance power transmission via submarine cables presents difficulties due to complex seabed topography, high laying costs, difficulties in cable maintenance, and high transmission costs, making cable transmission uneconomical. Furthermore, long-distance hydrogen storage and transportation are not economically feasible and pose significant safety risks. Summary of the Invention

[0004] The technical problem to be solved by the present invention is to address at least one of the defects of the related technologies mentioned in the background: the amount of carbon source required for the production of green synthetic fuels is small and the cost is high; the long-distance storage and transportation of liquid hydrogen is not economically feasible and poses high safety risks. The present invention provides a method and system for green energy conversion and utilization.

[0005] The technical solution adopted by this invention to solve its technical problem is: to construct a green energy conversion and utilization method, comprising the following steps: S1: The storage and transportation system analyzes the collected biomass / organic matter on-site, and performs corresponding pretreatment on the biomass / organic matter according to the analysis results to obtain at least one of compressed pellets, pyrolytic char and pyrolytic oil; S2: The green energy transfer and storage system generates electricity using green energy. At the same time, the compressed particles and pyrolysis char pre-treated from the storage and transportation system are fed into the gasification unit for gasification. The generated pyrolysis gas is combined with hydrogen generated from water electrolysis to produce green synthetic fuel. S3: The green electricity transfer and storage system will react the pyrolysis oil pretreated from the storage and transportation system with hydrogen generated from water electrolysis under high temperature and high pressure to perform a hydrogenation and deoxygenation upgrading reaction, thereby obtaining green finished oil.

[0006] In some embodiments, the storage and transportation system includes multi-level storage and transportation nodes, which include a first-level storage and transportation node, a second-level storage and transportation node, and a third-level storage and transportation node; The area represented by the third-level storage and transportation node is larger than the area represented by the second-level storage and transportation node, and the area represented by the second-level storage and transportation node is larger than the area represented by the first-level storage and transportation node.

[0007] In some embodiments, step S1 includes: Based on the origin of the collected biomass / organic matter, the collected biomass / organic matter is analyzed at the optimal storage and transportation node of the origin. Based on the analysis results, the biomass / organic matter is pretreated accordingly to obtain at least one of the compressed pellets, the pyrolysis char, and the pyrolysis oil.

[0008] In some embodiments, the determination of the optimal hierarchical storage and transportation node includes: The storage and transportation system aims to minimize transportation and storage costs. It comprehensively considers at least one of the following factors: the current available storage capacity and pre-processing capacity of each level of storage and transportation node, and whether the transportation vehicle is on the right route or takes a detour. It analyzes and calculates the feasibility and cost differences of transporting the biomass / organic matter to the selectable level of storage and transportation node, and determines the optimal level of storage and transportation node.

[0009] In some embodiments, step S1 includes: Based on the origin of the collected biomass / organic matter, the collected biomass / organic matter is analyzed at the highest-level storage and transportation node to which the origin belongs. Based on the analysis results, the biomass / organic matter is pretreated accordingly to obtain at least one of the compressed pellets, the pyrolysis char, and the pyrolysis oil.

[0010] In some embodiments, the collected biomass / organic matter is analyzed, and based on the analysis results, the biomass / organic matter is pretreated accordingly to obtain at least one of compressed pellets, pyrolysis char, and pyrolysis oil, including: The collected biomass / organic matter is subjected to industrial analysis. Based on evaluation factors, the economic transportation radius after crushing and compression is evaluated. If the biomass / organic matter has a radius greater than a preset distance, it is preferentially subjected to crushing and compression to obtain the compressed particles. The evaluation factors include, but are not limited to, at least one of the following: fixed carbon content, crushing and compression power consumption, and post-compression density. Elemental analysis was performed on the biomass / organic matter that was not suitable for crushing and compression. According to the elemental analysis results, the biomass / organic matter with a hydrogen-to-carbon ratio greater than 1 is subjected to a rapid high-temperature pyrolysis process to obtain the pyrolysis oil; The biomass / organic matter with an effective hydrogen-to-carbon ratio less than or equal to 1 is subjected to a low-temperature pyrolysis process to obtain the pyrolytic carbon.

[0011] In some embodiments, the pretreatment method includes the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process of cogeneration, which includes: The heat energy dissipated during cooling in the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process is used for the heat absorption portion of the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process, and / or for the heat absorption portion of the production process; and the non-condensable combustible gas produced by the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process is collected for combustion to maintain the pyrolysis reaction or production.

[0012] In some embodiments, the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process of cogeneration further include: Multiple heat sources and multiple heat-absorbing parts are matched for heat exchange pairs based on the principle of similar temperature.

[0013] In some embodiments, the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process of cogeneration further include: In the heat exchange scenario, the solid-side gas phase and the gas-side or liquid-side medium are exchanged through a coupling heat exchanger. The coupling heat exchanger replaces gas-solid heat exchange with gas-gas heat exchange and gas-solid mixing, and replaces liquid-solid heat exchange with liquid-gas heat exchange and gas-solid mixing. The heat exchange scenarios include, but are not limited to: heat exchange scenarios with multiple heat sources and a single heat-absorbing medium and / or heat exchange scenarios with a single heat source and multiple heat-absorbing media.

[0014] In some embodiments, the heat energy dissipated by cooling in the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process includes, but is not limited to, at least one of the following: the heat energy dissipated by cooling the pyrolysis gas produced by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis oil obtained by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis gas produced by the low-temperature pyrolysis process, and the heat energy dissipated by cooling the pyrolysis carbon obtained by the low-temperature pyrolysis process. The heat-absorbing parts of the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process include, but are not limited to: the preheating part and / or the pyrolysis part of the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process; The heat-absorbing parts of the production process include, but are not limited to: producing industrial steam and / or producing hot water; The non-condensable combustible gases include, but are not limited to: H2 and / or CO.

[0015] In some embodiments, the biomass / organic matter with a hydrogen-to-carbon ratio greater than 1, based on elemental analysis results, undergoes a rapid high-temperature pyrolysis process to obtain the pyrolysis oil; the biomass / organic matter with a hydrogen-to-carbon ratio less than or equal to 1 undergoes a low-temperature pyrolysis process to obtain the pyrolysis char, including: According to the elemental analysis results, the biomass / organic matter with a hydrogen-to-carbon ratio greater than 1 enters the rapid high-temperature pyrolysis device after being preheated by the first preheater. The pyrolysis gas flow generated by the rapid high-temperature pyrolysis device passes through the first preheater for auxiliary preheating, and then passes through the first cooler to obtain the pyrolysis oil and non-condensable combustible gas. The first cooler is connected to the first coupling heat exchanger through the first circulating pump to form a circulation loop, so as to transfer the heat released by cooling to the medium-temperature zone and the low-temperature zone of the first coupling heat exchanger. The first induced draft fan delivers the non-condensable combustible gas to the first combustion chamber. The flue gas generated in the first combustion chamber passes through the rapid high-temperature pyrolysis device to heat the device. The flue gas then enters the first coupled heat exchanger, where it undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling to ambient temperature. The rapid high-temperature pyrolysis device also produces ash, which enters the first coupled heat exchanger and undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling to ambient temperature. The biomass / organic matter with a hydrogen-to-carbon ratio less than or equal to 1 is preheated by the second preheater and then enters the low-temperature pyrolysis device to obtain the pyrolytic carbon. The pyrolysis gas flow generated by the low-temperature pyrolysis device is preheated by the second preheater and then enters the second cooler to obtain the non-condensable combustible gas. The second induced draft fan transports the non-condensable combustible gas to the first gasification device for combustion. The second cooler is connected to the first coupling heat exchanger through the second circulating pump to form a circulation loop to transfer the heat released by the cooling to the low-temperature zone of the first coupling heat exchanger. The first blower delivers ambient temperature air to the first coupling heat exchanger for heating, and finally outputs hot air to the rapid high-temperature pyrolysis device and / or the low-temperature pyrolysis device to heat the rapid high-temperature pyrolysis device and / or the low-temperature pyrolysis device. The second blower preheats the ambient temperature air through the third preheater and then delivers it to the first gasification unit; The first water pump delivers room temperature water to the low-temperature zone of the first coupling heat exchanger for heating, and then delivers it to the first gasification unit to absorb heat, thereby producing hot water or industrial steam.

[0016] In some embodiments, the green energy conversion and utilization method further includes: The storage and transportation system classifies and stores the obtained compressed granules, pyrolytic char, and pyrolytic oil in containers. Each container has a fixed unique identifier, and the administrator logs into the system by scanning the unique identifier and filling in relevant information. Among them, the administrator includes, but is not limited to, at least one of the following: origin administrator, transportation process administrator, and maintenance administrator; The information that the origin administrator can fill in includes, but is not limited to: the origin of the biomass / organic matter, a brief description of the economic transportation radius analysis of crushing and compression, the results of raw material element analysis, the pretreatment method, the pretreatment date, the elemental composition of the pretreated product, the calorific value of the pretreated product, and at least one of the following real-time statuses: empty or full. The information that the transportation process administrator can fill in includes, but is not limited to: the real-time status of each container and / or the location information of the storage and transportation nodes; The maintenance and repair administrator can fill in information including but not limited to: operating status and / or repair status information.

[0017] In some embodiments, the green electricity transfer and storage system feeds the pre-treated compressed pellets and pyrolytic char from the storage and transportation system into a gasification unit for gasification, including: The green electricity transfer and storage system feeds the compressed particles and pyrolytic char, which have been pretreated from the storage and transportation system, into the gasification unit for gasification according to their elemental composition.

[0018] In some embodiments, the components are proportioned according to their elemental composition and fed into the gasification device for gasification, including: The ratio of the two materials is calculated based on the effective hydrogen-to-carbon ratio of the compressed particles and the pyrolytic carbon, and then fed into the gasification device for gasification.

[0019] In some embodiments, the target hydrogen-to-carbon effective ratio after gasification is x. If the hydrogen-to-carbon effective ratio of the compressed particles to be mixed is B1, where B1 is greater than x, and the hydrogen-to-carbon effective ratio of the pyrolytic carbon to be mixed is B2, where B2 is less than x, then the ratio of the two materials is (x-B2) / (B1-x). If both B1 and B2 are less than x, or both are greater than x, then there is no need for a ratio.

[0020] In some embodiments, the step of reacting the pretreated pyrolysis oil from the storage and transportation system with hydrogen generated from water electrolysis under high temperature and high pressure to undergo a hydrogenation and deoxygenation upgrading reaction to obtain green finished oil includes: The pyrolysis oil, after pretreatment from the storage and transportation system, undergoes a hydrogenation and deoxygenation reaction with hydrogen generated from water electrolysis under high temperature and pressure, thereby increasing the calorific value of the pyrolysis oil to above a preset value. After purification by distillation, a green finished oil product is obtained.

[0021] In some embodiments, steps S2 and S3 include: In the green electricity transfer and storage system, water is electrolyzed in an electrolytic cell to decompose hydrogen and oxygen. The hydrogen is compressed by a first compressor and stored in a first container, and the oxygen is compressed by a second compressor and stored in a second container. The oxygen in the second container is supplied to the gasification device. The compressed particles and pyrolytic carbon, pretreated from the storage and transportation system, are mixed in a mixer according to their elemental composition and then fed into the gasification device for gasification to obtain pyrolysis gas. The pyrolysis gas is compressed by a third compressor and then preheated together with hydrogen from the first container through a fourth preheater. After preheating, a synthesis reaction is carried out in a first-stage catalytic synthesis device. The resulting medium flows through the fourth preheater to assist in preheating and then enters the first condenser for heat release. The medium from the first condenser passes through a first coarse separation device and a first refining device to obtain the final green synthetic fuel. Water and the pyrolysis oil pretreated from the storage and transportation system are preheated by the seventh preheater and then reacted with hydrogen from the first container and preheated by the eighth preheater to undergo a hydrogenation and deoxygenation reaction. The resulting medium is preheated by the eighth and seventh preheaters and then enters the third condenser for heat release. The heat-released medium is then processed by the second coarse separation unit and the second refining unit to obtain the final green finished oil. The first condenser is connected to the second coupled heat exchanger via a third circulating pump to form a circulation loop, so as to transfer heat to the low temperature zone of the second coupled heat exchanger; the third condenser is connected to the second coupled heat exchanger via a fifth circulating pump to form a circulation loop, so as to transfer heat to the medium temperature zone of the second coupled heat exchanger. The second feed water pump delivers ambient temperature demineralized water to the low temperature and medium temperature zones of the second coupling heat exchanger for heating, and then delivers it to the second gasification unit for further heating to produce hot water or industrial steam; the third blower delivers ambient temperature air to the second gasification unit after preheating it through the sixth preheater. The gasification device also produces ash residue, which enters the second coupled heat exchanger. The ash residue undergoes heat exchange in the medium-temperature zone and low-temperature zone of the second coupled heat exchanger, and finally cools down to room temperature.

[0022] In some embodiments, the green electricity storage system is a deep-sea energy island; The green energy conversion and utilization method also includes: The deep-sea energy island, by combining the consumption data of multiple offshore refueling stations, predicts the amount of green synthetic fuel and green refined oil stored on-site, predicts the amount of green synthetic fuel and green refined oil transported by ship to land for use, and schedules the amount of green synthetic fuel and green refined oil stored at the multiple offshore refueling stations.

[0023] In some embodiments, the green energy conversion and utilization method further includes: The green energy storage system estimates the scale of the power generation equipment to be deployed based on the resource information collected by the wind and solar measurement devices, as well as the hourly output of the power generation equipment, thereby calculating the combined hourly output of wind power and photovoltaic power, and then calculating the average output by combining the combined hourly output over a 24-hour period. Based on the difference between the comprehensive hourly output and the average output, the energy value that needs to be continuously stored and discharged or continuously stored and absorbed is determined, wherein the larger of the energy value of continuous energy storage discharge and the energy value of continuous energy storage absorption is taken as the energy storage capacity.

[0024] The present invention also constructs a green energy conversion and utilization system, including a storage and transportation system and a green electricity transfer and storage system. The storage and transportation system includes a pretreatment module, and the green electricity transfer and storage system includes a new energy power generation module, a water electrolysis and hydrogen-oxygen storage module, and a synthesis reaction module. The pretreatment module is configured to: analyze the collected biomass / organic matter on-site, and pretreat the biomass / organic matter accordingly based on the analysis results to obtain at least one of compressed pellets, pyrolytic char, and pyrolytic oil; The new energy power generation module is configured to generate electricity using green energy. The water electrolysis and hydrogen-oxygen storage module is configured to: electrolyze water to generate hydrogen and store hydrogen; The synthesis reaction module is configured to: feed the compressed particles and the pyrolysis char into a gasification device for gasification, and react the generated pyrolysis gas with hydrogen generated from water electrolysis to obtain green synthetic fuel; and react the pyrolysis oil with hydrogen generated from water electrolysis under high temperature and high pressure to undergo a hydrogenation and deoxygenation upgrading reaction to obtain green finished oil.

[0025] By implementing this invention, the following beneficial effects are achieved: This invention employs a pretreatment technology that reduces storage and transportation costs, coupled with a green electricity transfer and storage system that uses water electrolysis to generate hydrogen to synthesize green synthetic fuels and green refined oil products. This technology enables on-site pretreatment of collected biomass / organic matter within the storage and transportation system, thereby increasing the carbon content and energy density per unit volume of biomass / organic matter, reducing transportation costs, and expanding the storage radius. It can economically and on a large scale provide carbon sources for the conversion of green electricity into green synthetic fuels and green refined oil products, achieving more efficient, economical, and safer transmission and storage of renewable energy. Attached Figure Description

[0026] The present invention will be further described below with reference to the accompanying drawings and embodiments. In the accompanying drawings: Figure 1 A flowchart of the green energy conversion and utilization method of the present invention is shown; Figure 2 This invention illustrates a flowchart of the land-based pretreatment of biomass / organic matter in the green energy conversion and utilization method. Figure 3 This invention illustrates a flowchart of the marine synthesis of green synthetic fuels and green refined oil products in the green energy conversion and utilization method. Figure 4 The logical structure diagram of the green energy conversion and utilization system of the present invention is shown. Detailed Implementation

[0027] To provide a clearer understanding of the technical features, objectives, and effects of the present invention, specific embodiments of the present invention will now be described in detail with reference to the accompanying drawings.

[0028] It should be noted that the flowcharts shown in the accompanying drawings are merely illustrative and do not necessarily include all content and operations / steps, nor do they necessarily have to be performed in the described order. For example, some operations / steps can be broken down, while others can be combined or partially combined; therefore, the actual execution order may change depending on the specific circumstances.

[0029] The block diagrams shown in the accompanying drawings are merely functional entities and do not necessarily correspond to physically independent entities. That is, these functional entities can be implemented in software, in one or more hardware modules or integrated circuits, or in different network and / or processor devices and / or microcontroller devices.

[0030] It should be noted that at least one of the following can be one, two, three or any number.

[0031] First embodiment, such as Figure 1 As shown, this invention discloses a method for green energy conversion and utilization, including steps S1, S2, and S3, as detailed below: S1: The storage and transportation system analyzes the collected biomass / organic matter on-site. Based on the analysis results, it pre-processes the biomass / organic matter to obtain at least one of compressed pellets, pyrolysis char, and pyrolysis oil, thereby increasing the carbon content and energy density per unit volume of the biomass / organic matter, reducing transportation costs, and expanding the storage radius. For example, the storage and transportation system is a land-based storage and transportation system.

[0032] Related technologies supply carbon sources necessary for the production of green synthetic fuels and green refined oil products through methods such as air carbon capture, carbon capture from exhaust gases from supplementary combustion energy, salvaging and collecting biomass from the waters surrounding deep-sea energy islands (the biomass yield in the waters is large but dispersed and difficult to salvage in large quantities and stably, and its water content is extremely high, making pretreatment difficult and its value low), or long-distance transportation of untreated biomass / organic matter from land. These methods are either costly or have insufficient supply. However, this invention can economically and on a large scale provide carbon sources for the conversion of green electricity (such as deep-sea green electricity) into green synthetic fuels and green refined oil products, solving the problems of high carbon source cost and insufficient carbon source supply.

[0033] The storage and transportation system comprises multi-level storage and transportation nodes, including first-level, second-level, and third-level nodes. The area represented by a third-level node is larger than that represented by a second-level node, and vice versa. For example, in a land-based system, the first-level nodes are village-level, the second-level are town-level, and the third-level are county / regional. The collected biomass / organic matter is analyzed on-site at these nodes. Based on the analysis results, the biomass / organic matter undergoes appropriate pretreatment before being transported to the green energy transfer system. For instance, if the system is land-based and the green energy transfer system is a deep-sea energy island, the pretreated products can be transported from the port to the deep-sea energy island.

[0034] Step S1 specifically includes: analyzing the collected biomass / organic matter at the optimal tier storage and transportation node of the origin of the collected biomass / organic matter, and performing corresponding pretreatment on the biomass / organic matter based on the analysis results to obtain at least one of compressed pellets, pyrolysis char and pyrolysis oil.

[0035] The determination of the optimal tiered storage and transportation node includes: with the goal of minimizing storage and transportation costs, the storage and transportation system comprehensively considers at least one of the following factors: the current available storage capacity of each level of storage and transportation node, the pre-processing capacity, and whether the transportation vehicle (such as a transport vehicle) is on the right route or takes a detour. The feasibility and cost differences of transporting biomass / organic matter to the selectable tiered storage and transportation nodes are analyzed and calculated to determine the optimal tiered storage and transportation node.

[0036] Alternatively, step S1 may specifically include: analyzing the collected biomass / organic matter at the highest-level storage and transportation node (e.g., the third-level storage and transportation node) of the origin of the collected biomass / organic matter, and performing corresponding pretreatment on the biomass / organic matter based on the analysis results to obtain at least one of compressed pellets, pyrolytic char, and pyrolytic oil.

[0037] Biomass / organic matter includes, but is not limited to, at least one of the following: agricultural waste, agricultural product processing waste, wood processing waste, and industrial / domestic waste. Agricultural waste includes, but is not limited to, at least one of the following: rice straw, sorghum straw, broad bean straw, and cotton stalks. Agricultural product processing waste includes, but is not limited to, peanut shells and / or walnut shells. Wood processing waste includes, but is not limited to, wood scraps. Industrial / domestic waste includes, but is not limited to, plastics and / or kitchen waste.

[0038] Specifically, for storage and transportation nodes with suitable drying facilities, it is advisable to set up drying yards. Each drying yard can be equipped with reflectors or heat collection tanks to concentrate sunlight, thereby improving drying efficiency. This allows biomass / organic matter to be dried before further pretreatment processes. Urban solid waste needs to be sorted before drying to separate irrelevant waste, while kitchen waste needs to be dehydrated and spun dry before drying.

[0039] The process involves analyzing the collected biomass / organic matter, and pretreating it according to the analysis results to obtain at least one of compressed pellets, pyrolysis char, and pyrolysis oil, specifically including: The collected biomass / organic matter is subjected to industrial analysis. Based on the evaluation factors, the economic transportation radius after crushing and compression is evaluated. If the biomass / organic matter is greater than the preset distance (e.g., 200 kilometers), it is given priority for crushing and compression to obtain compressed pellets. The evaluation factors include, but are not limited to, at least one of the following: fixed carbon content, crushing and compression power consumption, and post-compression density. Elemental analysis was performed on biomass / organic matter that was not suitable for crushing and compression. Based on elemental analysis results, biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) greater than 1 can be processed using a rapid high-temperature pyrolysis process to obtain pyrolysis oil. Biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) less than or equal to 1 is subjected to low-temperature pyrolysis to obtain pyrolytic char.

[0040] Low-temperature pyrolysis refers to pyrolysis processes with temperatures between 200-350℃ and reaction times between 30-60 minutes. Rapid high-temperature pyrolysis refers to pyrolysis processes with temperatures between 450-650℃ and temperature changes of 1000-10000℃ / s per unit time.

[0041] To further reduce storage and transportation costs, a charcoal-oil cogeneration process is adopted, which includes pretreatment methods such as low-temperature pyrolysis and rapid high-temperature pyrolysis. Specifically, the charcoal-oil cogeneration process involves: utilizing the heat dissipated during cooling in the low-temperature and rapid high-temperature pyrolysis processes for the heat-absorbing portions of these processes, and / or for the heat-absorbing portions during production; and collecting the non-condensable combustible gases produced by the low-temperature and rapid high-temperature pyrolysis processes for combustion to sustain the pyrolysis reaction or production.

[0042] The heat energy dissipated by cooling in the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process includes at least one of the following: the heat energy dissipated by cooling the pyrolysis gas produced by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis oil obtained by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis gas produced by the low-temperature pyrolysis process, and the heat energy dissipated by cooling the pyrolysis carbon obtained by the low-temperature pyrolysis process.

[0043] The heat-absorbing parts in low-temperature pyrolysis and rapid high-temperature pyrolysis processes include, but are not limited to: the preheating part and / or the pyrolysis part in low-temperature pyrolysis and rapid high-temperature pyrolysis processes.

[0044] The heat-absorbing parts of the production process include, but are not limited to: the production of industrial steam and / or the production of hot water.

[0045] Non-condensable combustible gases include, but are not limited to: H2 (hydrogen) and / or CO (carbon monoxide).

[0046] In addition, the cogeneration process of charcoal and oil also includes matching multiple heat sources and multiple heat absorption parts according to the principle of similar temperature to make the heat energy utilized in stages.

[0047] The cogeneration process of charcoal and oil also includes: in heat exchange scenarios, heat exchange between the solid-side gas phase and the gas-side or liquid-side medium is carried out through a coupling heat exchanger. The coupling heat exchanger replaces gas-solid heat exchange with gas-gas heat exchange and gas-solid mixing, and replaces liquid-solid heat exchange with liquid-gas heat exchange and gas-solid mixing. The heat exchange scenarios include, but are not limited to: heat exchange scenarios with multiple heat sources and a single heat-absorbing medium and / or heat exchange scenarios with a single heat source and multiple heat-absorbing media.

[0048] Because the contact between solid raw materials and heat exchange surfaces is insufficient, coupled heat exchangers can be used to address the low efficiency of gas-solid and liquid-solid heat exchange. Coupled heat exchangers facilitate heat exchange between the solid-side gas phase and the gas-side or liquid-side medium, thereby ensuring thorough mixing and heat exchange between the solid-side gas phase and solid, thus improving heat exchange efficiency. Coupled heat exchangers replace gas-solid heat exchange with gas-gas heat exchange and gas-solid mixing, and liquid-solid heat exchange with liquid-gas heat exchange and gas-solid mixing, achieving strong coupling of heat exchange between the media on both sides of gas-solid and liquid-solid heat exchange. Coupled heat exchangers can also handle heat exchange scenarios with multiple heat sources and a single heat-absorbing medium, as well as a single heat source and multiple heat-absorbing media, reducing the overall heat dissipation of the process system and initial equipment investment.

[0049] Completely, as Figure 2 As shown, the collected biomass / organic matter is subjected to industrial analysis. Based on the evaluation factors, the economic transportation radius after crushing and compression is evaluated. If the biomass / organic matter is greater than the preset distance (e.g., 200 kilometers), it is given priority for crushing and compression to obtain compressed pellets. The evaluation factors include, but are not limited to, at least one of the following: fixed carbon content, crushing and compression power consumption, and density after compression. Elemental analysis was performed on biomass / organic matter that was not suitable for crushing and compression. According to elemental analysis results, biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) greater than 1 enters the rapid high-temperature pyrolysis unit after being preheated by the first preheater. The pyrolysis gas flow generated by the rapid high-temperature pyrolysis unit passes through the first preheater for auxiliary preheating, and then passes through the first cooler to obtain pyrolysis oil and non-condensable combustible gas (specifically, it first flows through a gas-solid separator to obtain pyrolysis carbon and gas, and the gas after gas-solid separation is then cooled by the first cooler to obtain pyrolysis oil and non-condensable combustible gas). The first cooler is connected to the first coupled heat exchanger through the first circulating pump to form a circulation loop, so as to transfer the heat released by cooling to the medium-temperature zone and low-temperature zone of the first coupled heat exchanger. The first induced draft fan delivers non-condensable combustible gas to the first combustion chamber. The flue gas generated in the first combustion chamber passes through a rapid high-temperature pyrolysis device to heat the device. The flue gas then enters the first coupling heat exchanger, where it undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling down to ambient temperature. The rapid high-temperature pyrolysis device also produces ash, which enters the first coupling heat exchanger. The ash undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling down to ambient temperature. After harmless treatment, the ash can be used in green energy storage systems, such as for land reclamation in deep-sea energy islands or as fertilizer for island greening. Biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) less than or equal to 1 is preheated in a second preheater and then enters a low-temperature pyrolysis unit to obtain pyrolytic carbon. In some embodiments, the pyrolytic carbon undergoes heat exchange in the medium-temperature and low-temperature zones of the first coupled heat exchanger, finally yielding room-temperature finished carbon. The pyrolysis gas flow generated by the low-temperature pyrolysis unit passes through the second preheater for auxiliary preheating and then enters the second cooler. After cooling, non-condensable combustible gas is obtained. A second induced draft fan transports the non-condensable combustible gas to the first gasification unit for combustion. The second cooler is connected to the first coupled heat exchanger via a second circulating pump to form a circulation loop, transferring the heat released during cooling to the low-temperature zone of the first coupled heat exchanger. The second cooler also produces wood vinegar and wood tar. The first blower delivers ambient temperature air to the first coupling heat exchanger for heating, and finally outputs hot air to the rapid high temperature pyrolysis device and / or low temperature pyrolysis device to heat the rapid high temperature pyrolysis device and / or low temperature pyrolysis device. The second blower preheats the ambient temperature air through the third preheater and then delivers it to the first gasification unit; The first feedwater pump delivers room temperature water to the low-temperature zone of the first coupling heat exchanger for heating, and then delivers it to the first gasification unit to absorb heat, thereby producing hot water or industrial steam and exhausting flue gas. The flue gas flows through the third preheater for heating and then is discharged into the atmosphere after being treated by environmental protection measures such as dust removal, desulfurization and denitrification.

[0050] It should be noted that the high-temperature zone, medium-temperature zone, and low-temperature zone of the first coupling heat exchanger are relative terms, and there is no specific definition of what the high-temperature, medium-temperature, and low-temperature zones are.

[0051] This green energy conversion and utilization method also includes: The storage and transportation system controls the state of low-temperature pyrolysis and rapid high-temperature pyrolysis processes by controlling the pyrolysis temperature rise rate and reaction time. This allows for the simultaneous improvement of carbon content and energy density per unit volume of biomass / organic matter, as well as carbon yield and hydrogen retention, while avoiding excessive energy loss due to over-pretreatment.

[0052] This green energy conversion and utilization method also includes: The storage and transportation system classifies and stores the obtained compressed granules, pyrolytic char, and pyrolytic oil in containers. Each container has a unique identifier, and the administrator logs into the system by scanning the unique identifier and filling in the relevant information.

[0053] For example, the container includes at least one of a container for storing liquids (such as pyrolytic oil) and an openable container for storing solids (such as compressed granules and pyrolytic char).

[0054] The containers have a fixed, unique identifier, such as a metal QR code nameplate welded onto the container. Alternatively, the storage and transportation containers use NFC technology, allowing the storage and transportation system to record the container identifier via electromagnetic induction.

[0055] Among them, the administrators include, but are not limited to, at least one of the following: origin administrator, transportation process administrator, and maintenance administrator. The permissions for each type of administrator to fill in information are different.

[0056] The information that the production site administrator can fill in includes, but is not limited to: the production site of biomass / organic matter, a brief description of the economic transportation radius analysis of crushing and compression, the results of raw material element analysis, the pretreatment method, the pretreatment date, the elemental composition of the pretreated product, the calorific value of the pretreated product, and at least one of the following real-time statuses: empty or full.

[0057] The information that the transportation process administrator can fill in includes, but is not limited to: the real-time status of each container and / or the location information of the storage and transportation nodes.

[0058] The information that maintenance and repair administrators can fill in includes, but is not limited to: operating status and / or repair status information.

[0059] like Figure 1 As shown, S2: The green electricity transfer system generates electricity using green energy (such as wind, solar, and wave energy). Simultaneously, pre-treated compressed pellets and pyrolysis char from the storage and transportation system are fed into a gasification unit for gasification. The resulting pyrolysis gas reacts with hydrogen produced from water electrolysis (i.e., hydrogen production from seawater electrolysis) to obtain green synthetic fuel, specifically green alcohol fuel (such as methanol). Understandably, the green electricity transfer system includes deep-sea energy islands and / or onshore energy bases. Deep-sea energy islands can utilize at least one of wind, solar, and wave energy, while onshore energy bases can utilize wind and / or solar energy. This invention is not only well-suited for green electricity transfer scenarios on deep-sea energy islands but also applicable to onshore wind power and photovoltaic power generation green electricity transfer scenarios.

[0060] Furthermore, the ash residue generated during the green synthetic fuel synthesis process can be used on-site for green electricity transfer and storage systems after being treated in a harmless manner, such as for land reclamation in deep-sea energy islands or as green fertilizer on the islands.

[0061] Step S2 specifically includes: the green electricity transfer and storage system takes the pre-treated compressed pellets and pyrolytic carbon from the storage and transportation system, and feeds them into the gasification unit (such as a gasifier with a pressure of 1.0-2.5 MPa and a temperature of 800-1000℃) according to their elemental composition for gasification. The pyrolysis gas produced is filtered and purified, and then reacted with hydrogen produced by water electrolysis to obtain green synthetic fuel.

[0062] The ratio of the two materials (H / Ceff) is calculated based on the hydrogen-to-carbon ratio (H / Ceff) of the compressed particles and the pyrolytic char before being fed into the gasification unit for gasification. For example, if the target H / Ceff after gasification is x, and the H / Ceff of the compressed particles to be mixed is B1 (B1 is greater than x), and the H / Ceff of the pyrolytic char to be mixed is B2 (B2 is less than x), then the ratio of the two materials is (x-B2) / (B1-x). If both B1 and B2 are less than x, or both are greater than x, then there is no need for mixing. The purpose of mixing is to keep the H / Ceff of the produced gas stable.

[0063] Compressed pellets or low-temperature pyrolysis char with low carbon content tend to reduce the carbon monoxide content in the gasification products within the gasification unit (e.g., gasifier), affecting reaction efficiency. Therefore, it is necessary to calculate the H / Ceff ratio based on the compressed pellets and pyrolysis char, and feed them into the gasification unit according to this ratio to stabilize the carbon monoxide and hydrogen content in the pyrolysis gas produced by the gasification unit, thereby improving gasification and synthesis efficiency. If the carbon monoxide content and flow rate fluctuate significantly while hydrogen is stably supplied to the gasification unit, the carbon monoxide and hydrogen ratio will fluctuate greatly. Sometimes carbon monoxide may not react completely, and sometimes hydrogen may not react completely, resulting in energy waste. The final synthesized green synthetic fuel has an H / Ceff atomic ratio slightly greater than 4. Because this H / Ceff can be ensured by hydrogen produced from water electrolysis, the gasification process only needs to maintain a stable H / Ceff. If it is unstable, it may lead to waste or insufficient subsequent hydrogen supply, thus affecting reaction efficiency.

[0064] like Figure 1 As shown, S3: The green energy transfer and storage system takes the pyrolysis oil pretreated from the storage and transportation system and reacts it with hydrogen generated from water electrolysis under high temperature and high pressure (e.g., temperature 300~400℃, pressure 10~20MPa) to produce green finished oil, such as green finished oil that is close to diesel.

[0065] Step S3 specifically includes: The green electricity transfer and storage system takes the pyrolysis oil pretreated from the storage and transportation system and reacts it with hydrogen generated from water electrolysis under high temperature and high pressure to carry out a hydrogenation and deoxygenation upgrading reaction, thereby increasing the calorific value of the pyrolysis oil to a preset value (for example, a preset value of 40 MJ / kg), and then obtains green finished oil after distillation to remove impurities.

[0066] For deep-sea energy islands far from land, transmitting electricity via submarine cables is not feasible. In scenarios where long-distance power transmission is inconvenient in the deep sea, establishing a comprehensive marine energy hub based on these deep-sea energy islands can facilitate the local consumption of electricity and its conversion into chemical energy (green synthetic fuels and green refined oil products). This can solve the problem of long-distance energy transmission. The underlying logic is to use "biomass / organic matter storage and transportation + methanol / bio-oil storage and transportation" to replace "liquid hydrogen or liquid ammonia storage and transportation" or "long-distance power transmission." This not only increases the added value of biomass / organic matter but also fully utilizes deep-sea renewable energy, expanding the scope of marine energy utilization in space and achieving more efficient, economical, and safer transmission and storage of deep-sea renewable energy.

[0067] Green synthetic fuels and green refined oil products can be used to refuel passing ships or transport them back to land. Compared with liquid hydrogen and liquid ammonia (liquid hydrogen solution: liquefying 1kg of hydrogen consumes 13-15 kWh of electricity, storage and transportation are difficult, costly, and dangerous, with one-thousandth evaporating every day; liquid ammonia solution: currently not easy to use as vehicle and ship fuel), green synthetic fuels and green refined oil products have relatively lower storage and transportation costs and safety risks, and have a larger application market.

[0068] Completely, as Figure 3 As shown, in the green electricity transfer and storage system, water is electrolyzed in an electrolyzer to decompose hydrogen and oxygen. The hydrogen is compressed by a first compressor and stored in a first container (such as a high-pressure storage tank). The oxygen is compressed by a second compressor and stored in a second container (such as a high-pressure storage tank). The oxygen in the second container is supplied to the gasification device. Compressed pellets and pyrolytic carbon, pretreated from the storage and transportation system, are mixed in a mixer according to their elemental composition and then fed into a gasification unit for gasification to obtain pyrolysis gas. The pyrolysis gas is compressed by a third compressor and then preheated together with hydrogen from the first container through a fourth preheater. After preheating, the gas undergoes a synthesis reaction in a first-stage catalytic synthesis unit (e.g., a first-stage catalytic synthesis tower at 200~380℃ and 6~12MPa). The resulting medium flows through the fourth preheater for auxiliary preheating and then enters the first condenser for exothermic reaction. The medium exiting the first condenser passes through a first coarse separation unit (e.g., a coarse separation tower) and a first refining unit (e.g., a refining tower) to obtain the final green synthetic fuel. Alternatively, the medium from the first condenser can be preheated by the fifth preheater through the first circulating compressor and then enter the secondary catalytic synthesis unit (such as a secondary catalytic synthesis tower with a temperature of 200~380℃ and a pressure of 6~12MPa) for synthesis reaction. The generated medium flows through the fifth preheater for auxiliary preheating and then enters the second condenser for heat release. The medium from the second condenser passes through the first coarse separation unit and the first refining unit to obtain the final green synthetic fuel. The second condenser is also connected to the first circulating compressor, and there is also a vent gas to the second combustion chamber. The medium after exiting the second combustion chamber flows through the gasification device, mixer and the sixth preheater for auxiliary heating. The flue gas discharged after passing through the sixth preheater is treated by environmental protection measures such as dust removal, desulfurization and denitrification before being discharged into the atmosphere. Water and pyrolysis oil pretreated from the storage and transportation system are preheated in the seventh preheater and then undergo a hydrogenation and deoxygenation reaction with hydrogen from the first container and preheated in the eighth preheater (300~400℃, 10~20MPa). The resulting medium is fed into the third condenser after being preheated by the eighth and seventh preheaters for further heat release. The heated medium then passes through the second coarse separation unit (e.g., coarse separation tower) and the second refining unit (e.g., refining tower) to obtain the final green finished oil. The heat required for the hydrogenation and deoxygenation reaction is provided by a circulation loop formed by a low-temperature molten salt tank, a molten salt heater, and a high-temperature molten salt tank. The third condenser is also connected to the eighth preheater via the second circulating compressor, and there is also a vent gas route to the second gas unit; The first condenser is connected to the second coupled heat exchanger via the third circulating pump to form a circulation loop, so as to transfer heat to the low temperature zone of the second coupled heat exchanger; the second condenser is connected to the second coupled heat exchanger via the fourth circulating pump to form a circulation loop, so as to transfer heat to the low temperature zone of the second coupled heat exchanger; the third condenser is connected to the second coupled heat exchanger via the fifth circulating pump to form a circulation loop, so as to transfer heat to the medium temperature zone of the second coupled heat exchanger. The second feedwater pump delivers ambient temperature demineralized water to the low-temperature and medium-temperature zones of the second coupling heat exchanger for heating, and then delivers it to the second gasification unit for further heating to produce hot water or industrial steam and exhaust flue gas. The flue gas flows through the sixth preheater for heating and is then sent to the air. After being treated by environmental protection measures such as dust removal, desulfurization, and denitrification, it is discharged into the atmosphere. The third blower delivers ambient temperature air to the second gasification unit after preheating it through the sixth preheater. The gasification unit also produces ash and slag, which enters the second coupled heat exchanger. The ash and slag undergo heat exchange in the medium-temperature zone and low-temperature zone of the second coupled heat exchanger, and finally cools down to room temperature.

[0069] When the green energy conversion and storage system is a deep-sea energy island, the green energy conversion and utilization method also includes: Some of the green synthetic fuels and green refined oil products are stored on deep-sea energy islands, some are stored at offshore refueling stations, and some are transported back to land by ship.

[0070] When the green energy conversion and storage system is a deep-sea energy island, the green energy conversion and utilization method also includes: The deep-sea energy island, by combining the consumption data of multiple offshore refueling stations, predicts the amount of green synthetic fuel and green refined oil stored on-site, predicts the amount of green synthetic fuel and green refined oil transported by ship to land for use, and coordinates the amount of green synthetic fuel and green refined oil stored at multiple offshore refueling stations.

[0071] This green energy conversion and utilization method also includes: The green energy storage system estimates the scale of the planned power generation units based on resource data collected by wind and solar measurement devices, as well as the hourly output of these units. This allows for the calculation of the combined hourly output of wind and solar power, which in turn is combined with the combined hourly output over a 24-hour period to calculate the average output. Similarly, when the green energy storage system is located in a deep-sea energy island, it estimates the scale of the planned power generation units based on resource data collected by wind, solar, and wave measurement devices, as well as the hourly output of these units. This allows for the calculation of the combined hourly output of wind, solar, and wave power, which in turn is combined with the combined hourly output over a 24-hour period to calculate the average output. Based on the difference between the comprehensive hourly output and the average output, the energy value that needs to be continuously stored for discharge or continuously stored for consumption is determined, and the larger of the energy value of continuous energy storage discharge and the energy value of continuous energy storage consumption is taken as the energy storage capacity.

[0072] Energy storage is achieved through a complementary combination of electricity and heat, while renewable energy is primarily wind power, which is converted into both electricity and heat. A portion of the electricity is used to stabilize the grid output during the islanded grid construction process of the green electricity transfer and storage system, while another portion is used to stabilize the hydrogen produced by water electrolysis. Of the hydrogen produced from water electrolysis, some is stored in pressure-stabilized tanks, some participates in the green synthetic fuel synthesis tower, and some participates in the hydrogenation and upgrading reaction of pyrolysis oil. The heat is used to maintain the temperatures required for the endothermic processes of gasification of compressed pellets and pyrolysis char, purification after gasification, and the synthesis of green synthetic fuels.

[0073] Therefore, electricity can be used to produce hydrogen, and heat can be used in the synthesis process. Considering the high cost and short lifespan of electricity storage, and the slightly lower cost and longer lifespan of thermal storage, the ratio of electricity storage to thermal storage should be optimized to reduce the capacity of electricity storage and lower investment costs.

[0074] This green energy conversion and utilization method also includes: Data from all stages of the storage and transportation system and the green electricity transfer system are collected, stored in the cloud, and displayed in real time.

[0075] The above is a description of the first embodiment (a method for converting and utilizing green energy), and the following is a description of the second embodiment (a system for converting and utilizing green energy).

[0076] In the second embodiment, such as Figure 4As shown, this invention discloses a green energy conversion and utilization system, including a storage and transportation system and a green electricity storage system. For example, the storage and transportation system is a land-based storage and transportation system, and the green electricity storage system includes a deep-sea energy island and / or a land-based energy base. The deep-sea energy island can utilize at least one of wind energy, solar energy, and wave energy, and the land-based energy base can utilize wind energy and / or solar energy. This invention is not only well applied to green electricity storage scenarios on deep-sea energy islands, but also applicable to green electricity storage scenarios such as onshore wind power generation and photovoltaic power generation. The storage and transportation system includes a pretreatment module, and the green electricity storage system includes a new energy power generation module, a water electrolysis and hydrogen-oxygen storage module, and a synthesis reaction module, as detailed below: The pretreatment module is configured to: analyze the collected biomass / organic matter on-site, and pretreat the biomass / organic matter according to the analysis results to obtain at least one of compressed pellets, pyrolysis char and pyrolysis oil, thereby increasing the carbon content and energy density per unit volume of biomass / organic matter, reducing transportation costs, and expanding the collection and storage radius.

[0077] Related technologies supply carbon sources necessary for the production of green synthetic fuels and green refined oil products through methods such as air carbon capture, carbon capture from exhaust gases from supplementary combustion energy, salvaging and collecting biomass from the waters surrounding deep-sea energy islands (the biomass yield in the waters is large but dispersed and difficult to salvage in large quantities and stably, and the water content is extremely high, making pretreatment difficult and the value low), or long-distance transportation of untreated biomass / organic matter from land. These methods are either costly or have insufficient supply. However, this invention can economically and on a large scale provide carbon sources for the conversion of green electricity into green synthetic fuels and green refined oil products, solving the problems of high carbon source cost and insufficient carbon source supply.

[0078] like Figure 4 As shown, the storage and transportation system also includes a warehousing and logistics module, which comprises multi-level storage and transportation nodes, including first-level, second-level, and third-level nodes. The area represented by a third-level node is larger than that represented by a second-level node, and vice versa. For example, in a land-based storage and transportation system, the first-level nodes are village-level, the second-level nodes are town-level, and the third-level nodes are county / regional-level. The pre-processing module at each storage and transportation node analyzes the collected biomass / organic matter on-site. Based on the analysis results, the biomass / organic matter is pre-processed accordingly, and the pre-processed products can be transported from the port to the green energy transfer and storage system. For instance, if the storage and transportation system is a land-based system and the green energy transfer and storage system is a deep-sea energy island, the pre-processed products can be transported from the port to the deep-sea energy island.

[0079] The storage and transportation system includes optimal hierarchical storage and transportation nodes based on the origin of the collected biomass / organic matter. The pretreatment module of the optimal hierarchical storage and transportation node is configured to analyze the collected biomass / organic matter and perform corresponding pretreatment on the biomass / organic matter based on the analysis results to obtain at least one of compressed pellets, pyrolytic char, and pyrolytic oil.

[0080] The determination of the optimal tiered storage and transportation node includes: with the goal of minimizing storage and transportation costs, the storage and transportation system comprehensively considers at least one of the following factors: the current available storage capacity of each level of storage and transportation node, the pre-processing capacity, and whether the transportation vehicle (such as a transport vehicle) is on the right route or takes a detour. The feasibility and cost differences of transporting biomass / organic matter to the selectable tiered storage and transportation nodes are analyzed and calculated to determine the optimal tiered storage and transportation node.

[0081] Alternatively, the storage and transportation system may include the highest-level storage and transportation node (e.g., the third-level storage and transportation node) based on the origin of the collected biomass / organic matter. The pretreatment module of the highest-level storage and transportation node is configured to analyze the collected biomass / organic matter and perform corresponding pretreatment on the biomass / organic matter based on the analysis results to obtain at least one of compressed pellets, pyrolytic char, and pyrolytic oil.

[0082] Biomass / organic matter includes, but is not limited to, at least one of the following: agricultural waste, agricultural product processing waste, wood processing waste, and industrial / domestic waste. Agricultural waste includes, but is not limited to, at least one of the following: rice straw, sorghum straw, broad bean straw, and cotton stalks. Agricultural product processing waste includes, but is not limited to, peanut shells and / or walnut shells. Wood processing waste includes, but is not limited to, wood scraps. Industrial / domestic waste includes, but is not limited to, plastics and / or kitchen waste.

[0083] Specifically, for storage and transportation nodes with suitable drying facilities, it is advisable to set up drying yards. Each drying yard can be equipped with reflectors or heat collection tanks to concentrate sunlight, thereby improving drying efficiency. This allows biomass / organic matter to be dried before further pretreatment processes. Urban solid waste needs to be sorted before drying to separate irrelevant waste, while kitchen waste needs to be dehydrated and spun dry before drying.

[0084] The process involves analyzing the collected biomass / organic matter, and pretreating it according to the analysis results to obtain at least one of compressed pellets, pyrolysis char, and pyrolysis oil, specifically including: The collected biomass / organic matter is subjected to industrial analysis. Based on the evaluation factors, the economic transportation radius after crushing and compression is evaluated. If the biomass / organic matter is greater than the preset distance (e.g., 200 kilometers), it is given priority for crushing and compression to obtain compressed pellets. The evaluation factors include, but are not limited to, at least one of the following: fixed carbon content, crushing and compression power consumption, and post-compression density. Elemental analysis was performed on biomass / organic matter that was not suitable for crushing and compression. Based on elemental analysis results, biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) greater than 1 can be processed using a rapid high-temperature pyrolysis process to obtain pyrolysis oil. Biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) less than or equal to 1 is subjected to low-temperature pyrolysis to obtain pyrolytic char.

[0085] Low-temperature pyrolysis refers to pyrolysis processes with temperatures between 200-350℃ and reaction times between 30-60 minutes. Rapid high-temperature pyrolysis refers to pyrolysis processes with temperatures between 450-650℃ and temperature changes of 1000-10000℃ / s per unit time.

[0086] To further reduce storage and transportation costs, a charcoal-oil cogeneration process is adopted, which includes pretreatment methods such as low-temperature pyrolysis and rapid high-temperature pyrolysis. Specifically, the charcoal-oil cogeneration process involves: utilizing the heat dissipated during cooling in the low-temperature and rapid high-temperature pyrolysis processes for the heat-absorbing portions of these processes, and / or for the heat-absorbing portions during production; and collecting the non-condensable combustible gases produced by the low-temperature and rapid high-temperature pyrolysis processes for combustion to sustain the pyrolysis reaction or production.

[0087] The heat energy dissipated by cooling in the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process includes at least one of the following: the heat energy dissipated by cooling the pyrolysis gas produced by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis oil obtained by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis gas produced by the low-temperature pyrolysis process, and the heat energy dissipated by cooling the pyrolysis carbon obtained by the low-temperature pyrolysis process.

[0088] The heat-absorbing parts in low-temperature pyrolysis and rapid high-temperature pyrolysis processes include, but are not limited to: the preheating part and / or the pyrolysis part in low-temperature pyrolysis and rapid high-temperature pyrolysis processes.

[0089] The heat-absorbing parts of the production process include, but are not limited to: the production of industrial steam and / or the production of hot water.

[0090] Non-condensable combustible gases include, but are not limited to: H2 (hydrogen) and / or CO (carbon monoxide).

[0091] In addition, the cogeneration process of charcoal and oil also includes matching multiple heat sources and multiple heat absorption parts according to the principle of similar temperature to make the heat energy utilized in stages.

[0092] The cogeneration process of charcoal and oil also includes: in heat exchange scenarios, heat exchange between the solid-side gas phase and the gas-side or liquid-side medium is carried out through a coupling heat exchanger. The coupling heat exchanger replaces gas-solid heat exchange with gas-gas heat exchange and gas-solid mixing, and replaces liquid-solid heat exchange with liquid-gas heat exchange and gas-solid mixing. The heat exchange scenarios include, but are not limited to: heat exchange scenarios with multiple heat sources and a single heat-absorbing medium and / or heat exchange scenarios with a single heat source and multiple heat-absorbing media.

[0093] Because the contact between solid raw materials and heat exchange surfaces is insufficient, coupled heat exchangers can be used to address the low efficiency of gas-solid and liquid-solid heat exchange. Coupled heat exchangers facilitate heat exchange between the solid-side gas phase and the gas-side or liquid-side medium, thereby ensuring thorough mixing and heat exchange between the solid-side gas phase and solid, thus improving heat exchange efficiency. Coupled heat exchangers replace gas-solid heat exchange with gas-gas heat exchange and gas-solid mixing, and liquid-solid heat exchange with liquid-gas heat exchange and gas-solid mixing, achieving strong coupling of heat exchange between the media on both sides of gas-solid and liquid-solid heat exchange. Coupled heat exchangers can also handle heat exchange scenarios with multiple heat sources and a single heat-absorbing medium, as well as a single heat source and multiple heat-absorbing media, reducing the overall heat dissipation of the process system and initial equipment investment.

[0094] Completely, as Figure 2 As shown, the preprocessing module is configured as follows: The collected biomass / organic matter is subjected to industrial analysis. Based on the evaluation factors, the economic transportation radius after crushing and compression is evaluated. If the biomass / organic matter is greater than the preset distance (e.g., 200 kilometers), it is given priority for crushing and compression to obtain compressed pellets. The evaluation factors include, but are not limited to, at least one of the following: fixed carbon content, crushing and compression power consumption, and post-compression density. Elemental analysis was performed on biomass / organic matter that was not suitable for crushing and compression. According to elemental analysis results, biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) greater than 1 enters the rapid high-temperature pyrolysis unit after being preheated by the first preheater. The pyrolysis gas flow generated by the rapid high-temperature pyrolysis unit passes through the first preheater for auxiliary preheating, and then passes through the first cooler to obtain pyrolysis oil and non-condensable combustible gas (specifically, it first flows through a gas-solid separator to obtain pyrolysis carbon and gas, and the gas after gas-solid separation is then cooled by the first cooler to obtain pyrolysis oil and non-condensable combustible gas). The first cooler is connected to the first coupled heat exchanger through the first circulating pump to form a circulation loop, so as to transfer the heat released by cooling to the medium-temperature zone and low-temperature zone of the first coupled heat exchanger. The first induced draft fan delivers non-condensable combustible gas to the first combustion chamber. The flue gas generated in the first combustion chamber passes through a rapid high-temperature pyrolysis device to heat the device. The flue gas then enters the first coupling heat exchanger, where it undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling down to ambient temperature. The rapid high-temperature pyrolysis device also produces ash, which enters the first coupling heat exchanger. The ash undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling down to ambient temperature. After harmless treatment, the ash can be used in green energy storage systems, such as for land reclamation in deep-sea energy islands or as fertilizer for island greening. Biomass / organic matter with a hydrogen-to-carbon ratio (H / Ceff) less than or equal to 1 is preheated in a second preheater and then enters a low-temperature pyrolysis unit to obtain pyrolytic carbon. In some embodiments, the pyrolytic carbon undergoes heat exchange in the medium-temperature and low-temperature zones of the first coupled heat exchanger, finally yielding room-temperature finished carbon. The pyrolysis gas flow generated by the low-temperature pyrolysis unit passes through the second preheater for auxiliary preheating and then enters the second cooler. After cooling, non-condensable combustible gas is obtained. A second induced draft fan transports the non-condensable combustible gas to the first gasification unit for combustion. The second cooler is connected to the first coupled heat exchanger via a second circulating pump to form a circulation loop, transferring the heat released during cooling to the low-temperature zone of the first coupled heat exchanger. The second cooler also produces wood vinegar and wood tar. The first blower delivers ambient temperature air to the first coupling heat exchanger for heating, and finally outputs hot air to the rapid high temperature pyrolysis device and / or low temperature pyrolysis device to heat the rapid high temperature pyrolysis device and / or low temperature pyrolysis device. The second blower preheats the ambient temperature air through the third preheater and then delivers it to the first gasification unit; The first feedwater pump delivers room temperature water to the low-temperature zone of the first coupling heat exchanger for heating, and then delivers it to the first gasification unit to absorb heat, thereby producing hot water or industrial steam and exhausting flue gas. The flue gas flows through the third preheater for heating and then is discharged into the atmosphere after being treated by environmental protection measures such as dust removal, desulfurization and denitrification.

[0095] It should be noted that the high-temperature zone, medium-temperature zone, and low-temperature zone of the first coupling heat exchanger are relative terms, and there is no specific definition of what the high-temperature, medium-temperature, and low-temperature zones are.

[0096] The pretreatment module is also configured to control the state of low-temperature pyrolysis and rapid high-temperature pyrolysis processes by controlling the pyrolysis temperature rise rate and reaction time, thereby improving carbon yield and hydrogen retention while simultaneously increasing the carbon content and energy density per unit volume of biomass / organic matter, and avoiding excessive energy loss due to over-pretreatment.

[0097] The pretreatment module is also configured to classify and store the obtained compressed particles, pyrolytic char, and pyrolytic oil in containers. Each container has a unique identifier, and the administrator can log in to the system by scanning the unique identifier to fill in relevant information.

[0098] For example, the container includes at least one of a container for storing liquids (such as pyrolytic oil) and an openable container for storing solids (such as compressed granules and pyrolytic char).

[0099] The containers have a fixed, unique identifier, such as a metal QR code nameplate welded onto the container. Alternatively, the storage and transportation containers use NFC technology, allowing the storage and transportation system to record the container identifier via electromagnetic induction.

[0100] Among them, the administrators include, but are not limited to, at least one of the following: origin administrator, transportation process administrator, and maintenance administrator. The permissions for each type of administrator to fill in information are different.

[0101] The information that the production site administrator can fill in includes, but is not limited to: the production site of biomass / organic matter, a brief description of the economic transportation radius analysis of crushing and compression, the results of raw material element analysis, the pretreatment method, the pretreatment date, the elemental composition of the pretreated product, the calorific value of the pretreated product, and at least one of the following real-time statuses: empty or full.

[0102] The information that the transportation process administrator can fill in includes, but is not limited to: the real-time status of each container and / or the location information of the storage and transportation nodes.

[0103] The information that maintenance and repair administrators can fill in includes, but is not limited to: operating status and / or repair status information.

[0104] like Figure 4 As shown, the new energy power generation module is configured to generate electricity using green energy. The water electrolysis and hydrogen-oxygen storage module is configured to electrolyze water to produce and store hydrogen.

[0105] The synthesis reaction module is configured to feed the pre-treated compressed particles and pyrolytic carbon from the pretreatment module into the gasification unit for gasification. The resulting pyrolysis gas is then reacted with hydrogen produced by water electrolysis (i.e., hydrogen production from seawater electrolysis) to obtain green synthetic fuel, specifically green alcohol fuel (such as methanol).

[0106] Furthermore, the ash residue generated during the green synthetic fuel synthesis process can be used on-site for deep-sea energy islands after being treated in a harmless manner, such as for land reclamation or as green fertilizer on the islands.

[0107] The synthesis reaction module is further configured to: feed the compressed particles and pyrolytic carbon pretreated from the pretreatment module into a gasification device (such as a gasifier with a pressure of 1.0-2.5 MPa and a temperature of 800-1000℃) according to their elemental composition for gasification. The resulting pyrolysis gas is filtered and purified before being reacted with hydrogen generated from water electrolysis to obtain green synthetic fuel.

[0108] The ratio of the two materials (H / Ceff) is calculated based on the hydrogen-to-carbon ratio (H / Ceff) of the compressed particles and the pyrolytic char before being fed into the gasification unit for gasification. For example, if the target H / Ceff after gasification is x, and the H / Ceff of the compressed particles to be mixed is B1 (B1 is greater than x), and the H / Ceff of the pyrolytic char to be mixed is B2 (B2 is less than x), then the ratio of the two materials is (x-B2) / (B1-x). If both B1 and B2 are less than x, or both are greater than x, then there is no need for mixing. The purpose of mixing is to keep the H / Ceff of the produced gas stable.

[0109] Compressed pellets or low-temperature pyrolysis char with low carbon content tend to reduce the carbon monoxide content in the gasification products within the gasification unit (e.g., gasifier), affecting reaction efficiency. Therefore, it is necessary to calculate the H / Ceff ratio based on the compressed pellets and pyrolysis char, and feed them into the gasification unit according to this ratio to stabilize the carbon monoxide and hydrogen content in the pyrolysis gas produced by the gasification unit, thereby improving gasification and synthesis efficiency. If the carbon monoxide content and flow rate fluctuate significantly while hydrogen is stably supplied to the gasification unit, the carbon monoxide and hydrogen ratio will fluctuate greatly. Sometimes carbon monoxide may not react completely, and sometimes hydrogen may not react completely, resulting in energy waste. The final synthesized green synthetic fuel has an H / Ceff atomic ratio slightly greater than 4. Because this H / Ceff can be ensured by hydrogen produced from water electrolysis, the gasification process only needs to maintain a stable H / Ceff. If it is unstable, it may lead to waste or insufficient subsequent hydrogen supply, thus affecting reaction efficiency.

[0110] like Figure 4 As shown, the synthesis reaction module is also configured to: react the pyrolysis oil pretreated from the pretreatment module with hydrogen generated from water electrolysis under high temperature and high pressure (e.g., temperature 300~400℃, pressure 10~20MPa) to produce a hydrogenation and deoxygenation upgrading reaction, thereby obtaining green finished oil, such as green finished oil that is close to diesel.

[0111] The synthesis reaction module is further configured to: conduct a hydrogenation and deoxygenation upgrading reaction between the pyrolysis oil pretreated from the pretreatment module and hydrogen generated by water electrolysis under high temperature and high pressure, thereby increasing the calorific value of the pyrolysis oil to a preset value (e.g., a preset value of 40 MJ / kg), and then obtain green finished oil after distillation to remove impurities.

[0112] For deep-sea energy islands far from land, transmitting electricity via submarine cables is not feasible. In scenarios where long-distance power transmission is inconvenient in the deep sea, establishing a comprehensive marine energy hub based on these deep-sea energy islands can facilitate the local consumption of electricity and its conversion into chemical energy (green synthetic fuels and green refined oil products). This can solve the problem of long-distance energy transmission. The underlying logic is to use "biomass / organic matter storage and transportation + methanol / bio-oil storage and transportation" to replace "liquid hydrogen or liquid ammonia storage and transportation" or "long-distance power transmission." This not only increases the added value of biomass / organic matter but also fully utilizes deep-sea renewable energy, expanding the scope of marine energy utilization in space and achieving more efficient, economical, and safer transmission and storage of deep-sea renewable energy.

[0113] Green synthetic fuels and green refined oil products can be used to refuel passing ships or transport them back to land. Compared with liquid hydrogen and liquid ammonia (liquid hydrogen solution: liquefying 1kg of hydrogen consumes 13-15 kWh of electricity, storage and transportation are difficult, costly, and dangerous, with one-thousandth evaporating every day; liquid ammonia solution: currently not easy to use as vehicle and ship fuel), green synthetic fuels and green refined oil products have relatively lower storage and transportation costs and safety risks, and have a larger application market.

[0114] Completely, as Figure 3 As shown, the synthesis reaction module is configured as follows: In the green electricity transfer and storage system, water is electrolyzed in an electrolyzer to decompose it into hydrogen and oxygen. The hydrogen is compressed by a first compressor and stored in a first container (such as a high-pressure storage tank), while the oxygen is compressed by a second compressor and stored in a second container (such as a high-pressure storage tank). The oxygen in the second container is supplied to the gasification device. The pre-treated compressed particles and pyrolytic carbon from the pretreatment module are mixed in a mixer according to their elemental composition and then fed into a gasification unit for gasification to obtain pyrolysis gas. The pyrolysis gas is compressed by a third compressor and then preheated together with hydrogen from the first container through a fourth preheater. After preheating, the gas undergoes a synthesis reaction in a first-stage catalytic synthesis unit (e.g., a first-stage catalytic synthesis tower at 200~380℃ and 6~12MPa). The resulting medium flows through the fourth preheater for auxiliary preheating and then enters the first condenser for exothermic reaction. The medium exiting the first condenser passes through a first coarse separation unit (e.g., a coarse separation tower) and a first refining unit (e.g., a refining tower) to obtain the final green synthetic fuel. Alternatively, the medium from the first condenser can be preheated by the fifth preheater through the first circulating compressor and then enter the secondary catalytic synthesis unit (such as a secondary catalytic synthesis tower with a temperature of 200~380℃ and a pressure of 6~12MPa) for synthesis reaction. The generated medium flows through the fifth preheater for auxiliary preheating and then enters the second condenser for heat release. The medium from the second condenser passes through the first coarse separation unit and the first refining unit to obtain the final green synthetic fuel. The second condenser is also connected to the first circulating compressor, and there is also a vent gas to the second combustion chamber. The medium after exiting the second combustion chamber flows through the gasification device, mixer and the sixth preheater for auxiliary heating. The flue gas discharged after passing through the sixth preheater is treated by environmental protection measures such as dust removal, desulfurization and denitrification before being discharged into the atmosphere. Water and pyrolysis oil pretreated from the pretreatment module are preheated in the seventh preheater and then undergo a hydrogenation and deoxygenation reaction with hydrogen from the first container and preheated in the eighth preheater (300~400℃, 10~20MPa). The resulting medium is fed into the third condenser after being preheated by the eighth and seventh preheaters for further heat release. The heated medium then passes through the second coarse separation unit (e.g., coarse separation tower) and the second refining unit (e.g., refining tower) to obtain the final green finished oil. The heat required for the hydrogenation and deoxygenation reaction is provided by a circulation loop formed by the low-temperature molten salt tank, the molten salt heater, and the high-temperature molten salt tank. The third condenser is also connected to the eighth preheater via the second circulating compressor, and there is also a vent gas route to the second gas unit; The first condenser is connected to the second coupled heat exchanger via the third circulating pump to form a circulation loop, so as to transfer heat to the low temperature zone of the second coupled heat exchanger; the second condenser is connected to the second coupled heat exchanger via the fourth circulating pump to form a circulation loop, so as to transfer heat to the low temperature zone of the second coupled heat exchanger; the third condenser is connected to the second coupled heat exchanger via the fifth circulating pump to form a circulation loop, so as to transfer heat to the medium temperature zone of the second coupled heat exchanger. The second feedwater pump delivers ambient temperature demineralized water to the low-temperature and medium-temperature zones of the second coupling heat exchanger for heating, and then delivers it to the second gasification unit for further heating to produce hot water or industrial steam and exhaust flue gas. The flue gas flows through the sixth preheater for heating and is then sent to the air. After being treated by environmental protection measures such as dust removal, desulfurization, and denitrification, it is discharged into the atmosphere. The third blower delivers ambient temperature air to the second gasification unit after preheating it through the sixth preheater. The gasification unit also produces ash and slag, which enters the second coupled heat exchanger. The ash and slag undergo heat exchange in the medium-temperature zone and low-temperature zone of the second coupled heat exchanger, and finally cools down to room temperature.

[0115] like Figure 4 As shown, when the green electricity transfer and storage system is a deep-sea energy island, the green electricity transfer and storage system also includes a storage and transportation module. The storage and transportation module is configured such that: part of the green synthetic fuel and green refined oil are stored on the deep-sea energy island, part are stored at the offshore refueling station, and part are transported back to the land by ship.

[0116] like Figure 4As shown, when the green electricity transfer and storage system is a deep-sea energy island, the green electricity transfer and storage system also includes an offshore refueling station module. The offshore refueling station module is configured to: predict the amount of green synthetic fuel and green refined oil stored on-site by combining the consumption of multiple offshore refueling stations; predict the amount of green synthetic fuel and green refined oil transported by ship to land for use; and schedule the amount of green synthetic fuel and green refined oil stored at multiple offshore refueling stations. like Figure 4 As shown, the green electricity transfer and storage system also includes an energy storage and dispatch module, which is configured as follows: Based on the resource data collected by wind and solar measurement devices, the scale of the planned power generation equipment is estimated, along with the hourly output of the equipment. This allows for the calculation of the combined hourly output of wind and solar power, which in turn is combined with the combined hourly output over a 24-hour period to calculate the average output. Similarly, when the green energy storage system is a deep-sea energy island, the scale of the planned power generation equipment is estimated based on the resource data collected by wind, solar, and wave measurement devices, along with the hourly output of the equipment. This allows for the calculation of the combined hourly output of wind, solar, and wave power, which in turn is combined with the combined hourly output over a 24-hour period to calculate the average output. Based on the difference between the comprehensive hourly output and the average output, the energy value that needs to be continuously stored for discharge or continuously stored for consumption is determined, and the larger of the energy value of continuous energy storage discharge and the energy value of continuous energy storage consumption is taken as the energy storage capacity.

[0117] Energy storage is achieved through a complementary combination of electricity and heat, while renewable energy is primarily wind power, which is converted into both electricity and heat. A portion of the electricity is used to stabilize the grid output during the islanded grid construction process of the green electricity transfer and storage system, while another portion is used to stabilize the hydrogen produced by water electrolysis. Of the hydrogen produced from water electrolysis, some is stored in pressure-stabilized tanks, some participates in the green synthetic fuel synthesis tower, and some participates in the hydrogenation and upgrading reaction of pyrolysis oil. The heat is used to maintain the temperatures required for the endothermic processes of gasification of compressed pellets and pyrolysis char, purification after gasification, and the synthesis of green synthetic fuels.

[0118] Therefore, electricity can be used to produce hydrogen, and heat can be used in the synthesis process. Considering the high cost and short lifespan of electricity storage, and the slightly lower cost and longer lifespan of thermal storage, the ratio of electricity storage to thermal storage should be optimized to reduce the capacity of electricity storage and lower investment costs.

[0119] like Figure 4 As shown, the green energy conversion and utilization system also includes a big data control and management network platform. The big data control and management network platform is configured to: collect and summarize data information from each link in the storage and transportation system and the green electricity conversion and storage system, store it in the cloud, and realize the real-time display of data information.

[0120] By implementing this invention, the following beneficial effects are achieved: This invention employs a pretreatment technology that reduces storage and transportation costs, coupled with a green electricity transfer and storage system to generate hydrogen from water electrolysis to synthesize green synthetic fuels and green refined oil products. This technology enables on-site pretreatment of collected biomass / organic matter within the storage and transportation system, thereby increasing the carbon content and energy density per unit volume of biomass / organic matter, reducing transportation costs, and expanding the storage radius. It can economically and on a large scale provide carbon sources for the conversion of green electricity (such as deep-sea green electricity) into green synthetic fuels and green refined oil products, achieving more efficient, economical, and safer transfer and storage of renewable energy (such as deep-sea renewable energy).

[0121] It is understood that the above embodiments only illustrate some implementation methods of the present invention, and their descriptions are relatively specific and detailed, but they should not be construed as limiting the scope of the present invention. It should be noted that those skilled in the art can freely combine the above embodiments or technical features without departing from the concept of the present invention, and can also make several modifications and improvements, all of which fall within the protection scope of the present invention. That is, the embodiments described "in some embodiments" can be freely combined with any of the preceding and following embodiments. Therefore, all equivalent transformations and modifications made within the scope of the claims of the present invention should be covered by the claims of the present invention.

Claims

1. A method for green energy conversion and utilization, characterized in that, Includes the following steps: S1: The storage and transportation system analyzes the collected biomass / organic matter on-site, and performs corresponding pretreatment on the biomass / organic matter according to the analysis results to obtain at least one of compressed pellets, pyrolytic char and pyrolytic oil; S2: The green energy transfer and storage system generates electricity using green energy. At the same time, the compressed particles and pyrolysis char pre-treated from the storage and transportation system are fed into the gasification unit for gasification. The generated pyrolysis gas is combined with hydrogen generated from water electrolysis to produce green synthetic fuel. S3: The green electricity transfer and storage system will react the pyrolysis oil pretreated from the storage and transportation system with hydrogen generated from water electrolysis under high temperature and high pressure to perform a hydrogenation and deoxygenation upgrading reaction, thereby obtaining green finished oil.

2. The green energy conversion and utilization method according to claim 1, characterized in that, The storage and transportation system includes multi-level storage and transportation nodes, which include first-level storage and transportation nodes, second-level storage and transportation nodes, and third-level storage and transportation nodes. The area represented by the third-level storage and transportation node is larger than the area represented by the second-level storage and transportation node, and the area represented by the second-level storage and transportation node is larger than the area represented by the first-level storage and transportation node.

3. The green energy conversion and utilization method according to claim 2, characterized in that, Step S1 includes: Based on the origin of the collected biomass / organic matter, the collected biomass / organic matter is analyzed at the optimal storage and transportation node of the origin. Based on the analysis results, the biomass / organic matter is pretreated accordingly to obtain at least one of the compressed pellets, the pyrolysis char, and the pyrolysis oil.

4. The green energy conversion and utilization method according to claim 3, characterized in that, The determination of the optimal hierarchical storage and transportation node includes: The storage and transportation system aims to minimize transportation and storage costs. It comprehensively considers at least one of the following factors: the current available storage capacity and pre-processing capacity of each level of storage and transportation node, and whether the transportation vehicle is on the right route or takes a detour. It analyzes and calculates the feasibility and cost differences of transporting the biomass / organic matter to the selectable level of storage and transportation node, and determines the optimal level of storage and transportation node.

5. The green energy conversion and utilization method according to claim 2, characterized in that, Step S1 includes: Based on the origin of the collected biomass / organic matter, the collected biomass / organic matter is analyzed at the highest-level storage and transportation node to which the origin belongs. Based on the analysis results, the biomass / organic matter is pretreated accordingly to obtain at least one of the compressed pellets, the pyrolysis char, and the pyrolysis oil.

6. The green energy conversion and utilization method according to any one of claims 1, 3, or 5, characterized in that, The collected biomass / organic matter was analyzed, and based on the analysis results, the biomass / organic matter was pretreated accordingly to obtain at least one of compressed pellets, pyrolysis char, and pyrolysis oil, including: The collected biomass / organic matter is subjected to industrial analysis. Based on evaluation factors, the economic transportation radius after crushing and compression is evaluated. If the biomass / organic matter has a radius greater than a preset distance, it is preferentially subjected to crushing and compression to obtain the compressed particles. The evaluation factors include, but are not limited to, at least one of the following: fixed carbon content, crushing and compression power consumption, and post-compression density. Elemental analysis was performed on the biomass / organic matter that was not suitable for crushing and compression. According to the elemental analysis results, the biomass / organic matter with a hydrogen-to-carbon ratio greater than 1 is subjected to a rapid high-temperature pyrolysis process to obtain the pyrolysis oil; The biomass / organic matter with an effective hydrogen-to-carbon ratio less than or equal to 1 is subjected to a low-temperature pyrolysis process to obtain the pyrolytic carbon.

7. The green energy conversion and utilization method according to claim 6, characterized in that, The pretreatment methods include the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process of cogeneration, which include: The heat energy dissipated during cooling in the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process is used for the heat absorption portion of the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process, and / or for the heat absorption portion of the production process; and the non-condensable combustible gas produced by the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process is collected for combustion to maintain the pyrolysis reaction or production.

8. The green energy conversion and utilization method according to claim 7, characterized in that, The low-temperature pyrolysis process and the rapid high-temperature pyrolysis process of cogeneration further include: Multiple heat sources and multiple heat-absorbing parts are matched for heat exchange pairs based on the principle of similar temperature.

9. The green energy conversion and utilization method according to claim 7, characterized in that, The low-temperature pyrolysis process and the rapid high-temperature pyrolysis process of cogeneration further include: In the heat exchange scenario, the solid-side gas phase and the gas-side or liquid-side medium are exchanged through a coupling heat exchanger. The coupling heat exchanger replaces gas-solid heat exchange with gas-gas heat exchange and gas-solid mixing, and replaces liquid-solid heat exchange with liquid-gas heat exchange and gas-solid mixing. The heat exchange scenarios include, but are not limited to: heat exchange scenarios with multiple heat sources and a single heat-absorbing medium and / or heat exchange scenarios with a single heat source and multiple heat-absorbing media.

10. The green energy conversion and utilization method according to claim 7, characterized in that, The heat energy dissipated by cooling in the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process includes, but is not limited to, at least one of the following: the heat energy dissipated by cooling the pyrolysis gas produced by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis oil obtained by the rapid high-temperature pyrolysis process, the heat energy dissipated by cooling the pyrolysis gas produced by the low-temperature pyrolysis process, and the heat energy dissipated by cooling the pyrolysis carbon obtained by the low-temperature pyrolysis process. The heat-absorbing parts of the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process include, but are not limited to: the preheating part and / or the pyrolysis part of the low-temperature pyrolysis process and the rapid high-temperature pyrolysis process; The heat-absorbing parts of the production process include, but are not limited to: producing industrial steam and / or producing hot water; The non-condensable combustible gases include, but are not limited to: H2 and / or CO.

11. The green energy conversion and utilization method according to claim 9, characterized in that, According to the elemental analysis results, the biomass / organic matter with an effective hydrogen-to-carbon ratio greater than 1 is subjected to a rapid high-temperature pyrolysis process to obtain the pyrolysis oil; The biomass / organic matter with a hydrogen-to-carbon ratio less than or equal to 1 is subjected to a low-temperature pyrolysis process to obtain the pyrolytic char, comprising: According to the elemental analysis results, the biomass / organic matter with a hydrogen-to-carbon ratio greater than 1 enters the rapid high-temperature pyrolysis device after being preheated by the first preheater. The pyrolysis gas flow generated by the rapid high-temperature pyrolysis device passes through the first preheater for auxiliary preheating, and then passes through the first cooler to obtain the pyrolysis oil and non-condensable combustible gas. The first cooler is connected to the first coupling heat exchanger through the first circulating pump to form a circulation loop, so as to transfer the heat released by cooling to the medium-temperature zone and the low-temperature zone of the first coupling heat exchanger. The first induced draft fan delivers the non-condensable combustible gas to the first combustion chamber. The flue gas generated in the first combustion chamber passes through the rapid high-temperature pyrolysis device to heat the device. The flue gas then enters the first coupled heat exchanger, where it undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling to ambient temperature. The rapid high-temperature pyrolysis device also produces ash, which enters the first coupled heat exchanger and undergoes heat exchange in the high-temperature, medium-temperature, and low-temperature zones, finally cooling to ambient temperature. The biomass / organic matter with a hydrogen-to-carbon ratio less than or equal to 1 is preheated by the second preheater and then enters the low-temperature pyrolysis device to obtain the pyrolytic carbon. The pyrolysis gas flow generated by the low-temperature pyrolysis device is preheated by the second preheater and then enters the second cooler to obtain the non-condensable combustible gas. The second induced draft fan transports the non-condensable combustible gas to the first gasification device for combustion. The second cooler is connected to the first coupling heat exchanger through the second circulating pump to form a circulation loop to transfer the heat released by the cooling to the low-temperature zone of the first coupling heat exchanger. The first blower delivers ambient temperature air to the first coupling heat exchanger for heating, and finally outputs hot air to the rapid high-temperature pyrolysis device and / or the low-temperature pyrolysis device to heat the rapid high-temperature pyrolysis device and / or the low-temperature pyrolysis device. The second blower preheats the ambient temperature air through the third preheater and then delivers it to the first gasification unit; The first water pump delivers room temperature water to the low-temperature zone of the first coupling heat exchanger for heating, and then delivers it to the first gasification unit to absorb heat, thereby producing hot water or industrial steam.

12. The green energy conversion and utilization method according to claim 1, characterized in that, The green energy conversion and utilization method also includes: The storage and transportation system classifies and stores the obtained compressed granules, pyrolytic char, and pyrolytic oil in containers. Each container has a fixed unique identifier, and the administrator logs into the system by scanning the unique identifier and filling in relevant information. Among them, the administrator includes, but is not limited to, at least one of the following: origin administrator, transportation process administrator, and maintenance administrator; The information that the origin administrator can fill in includes, but is not limited to: the origin of the biomass / organic matter, a brief description of the economic transportation radius analysis of crushing and compression, the results of raw material element analysis, the pretreatment method, the pretreatment date, the elemental composition of the pretreated product, the calorific value of the pretreated product, and at least one of the following real-time statuses: empty or full. The information that the transportation process administrator can fill in includes, but is not limited to: the real-time status of each container and / or the location information of the storage and transportation nodes; The maintenance and repair administrator can fill in information including but not limited to: operating status and / or repair status information.

13. The green energy conversion and utilization method according to claim 1, characterized in that, The green electricity transfer and storage system feeds the pre-treated compressed pellets and pyrolytic char from the storage and transportation system into a gasification unit for gasification, including: The green electricity transfer and storage system feeds the compressed particles and pyrolytic char, which have been pretreated from the storage and transportation system, into the gasification unit for gasification according to their elemental composition.

14. The green energy conversion and utilization method according to claim 13, characterized in that, According to their elemental composition, they are mixed in proportion and fed into the gasification device for gasification, including: The ratio of the two materials is calculated based on the effective hydrogen-to-carbon ratio of the compressed particles and the pyrolytic carbon, and then fed into the gasification device for gasification.

15. The green energy conversion and utilization method according to claim 14, characterized in that, If the target hydrogen-to-carbon effective ratio after gasification is x, and the hydrogen-to-carbon effective ratio of the compressed particles to be mixed is B1, where B1 is greater than x, and the hydrogen-to-carbon effective ratio of the pyrolytic carbon to be mixed is B2, where B2 is less than x, then the ratio of the two materials is (x-B2) / (B1-x); if both B1 and B2 are less than x, or both are greater than x, then there is no need for a ratio.

16. The green energy conversion and utilization method according to claim 1, characterized in that, The process involves reacting the pretreated pyrolysis oil from the storage and transportation system with hydrogen generated from water electrolysis under high temperature and pressure for hydrogenation, deoxygenation, and upgrading to obtain green finished oil, including: The pyrolysis oil, after pretreatment from the storage and transportation system, undergoes a hydrogenation and deoxygenation reaction with hydrogen generated from water electrolysis under high temperature and pressure, thereby increasing the calorific value of the pyrolysis oil to above a preset value. After purification by distillation, a green finished oil product is obtained.

17. The green energy conversion and utilization method according to claim 1, characterized in that, Steps S2 and S3 include: In the green electricity transfer and storage system, water is electrolyzed in an electrolytic cell to decompose hydrogen and oxygen. The hydrogen is compressed by a first compressor and stored in a first container, and the oxygen is compressed by a second compressor and stored in a second container. The oxygen in the second container is supplied to the gasification device. The compressed particles and pyrolytic carbon, pretreated from the storage and transportation system, are mixed in a mixer according to their elemental composition and then fed into the gasification device for gasification to obtain pyrolysis gas. The pyrolysis gas is compressed by a third compressor and then preheated together with hydrogen from the first container through a fourth preheater. After preheating, a synthesis reaction is carried out in a first-stage catalytic synthesis device. The resulting medium flows through the fourth preheater to assist in preheating and then enters the first condenser for heat release. The medium from the first condenser passes through a first coarse separation device and a first refining device to obtain the final green synthetic fuel. Water and the pyrolysis oil pretreated from the storage and transportation system are preheated by the seventh preheater and then reacted with hydrogen from the first container and preheated by the eighth preheater to undergo a hydrogenation and deoxygenation reaction. The resulting medium is preheated by the eighth and seventh preheaters and then enters the third condenser for heat release. The heat-released medium is then processed by the second coarse separation unit and the second refining unit to obtain the final green finished oil. The first condenser is connected to the second coupled heat exchanger via a third circulating pump to form a circulation loop, so as to transfer heat to the low temperature zone of the second coupled heat exchanger; the third condenser is connected to the second coupled heat exchanger via a fifth circulating pump to form a circulation loop, so as to transfer heat to the medium temperature zone of the second coupled heat exchanger. The second feed water pump delivers ambient temperature demineralized water to the low temperature and medium temperature zones of the second coupling heat exchanger for heating, and then delivers it to the second gasification unit for further heating to produce hot water or industrial steam; the third blower delivers ambient temperature air to the second gasification unit after preheating it through the sixth preheater. The gasification device also produces ash residue, which enters the second coupled heat exchanger. The ash residue undergoes heat exchange in the medium-temperature zone and low-temperature zone of the second coupled heat exchanger, and finally cools down to room temperature.

18. The green energy conversion and utilization method according to claim 1, characterized in that, The green electricity transfer and storage system is a deep-sea energy island; The green energy conversion and utilization method also includes: The deep-sea energy island, by combining the consumption data of multiple offshore refueling stations, predicts the amount of green synthetic fuel and green refined oil stored on-site, predicts the amount of green synthetic fuel and green refined oil transported by ship to land for use, and schedules the amount of green synthetic fuel and green refined oil stored at the multiple offshore refueling stations.

19. The green energy conversion and utilization method according to claim 1, characterized in that, The green energy conversion and utilization method also includes: The green energy storage system estimates the scale of the power generation equipment to be deployed based on the resource information collected by the wind and solar measurement devices, as well as the hourly output of the power generation equipment, thereby calculating the combined hourly output of wind power and photovoltaic power, and then calculating the average output by combining the combined hourly output over a 24-hour period. Based on the difference between the comprehensive hourly output and the average output, the energy value that needs to be continuously stored and discharged or continuously stored and absorbed is determined, wherein the larger of the energy value of continuous energy storage discharge and the energy value of continuous energy storage absorption is taken as the energy storage capacity.

20. A green energy conversion and utilization system, characterized in that, It includes a storage and transportation system and a green electricity transfer and storage system. The storage and transportation system includes a pretreatment module, and the green electricity transfer and storage system includes a new energy power generation module, a water electrolysis and hydrogen-oxygen storage module, and a synthesis reaction module. The pretreatment module is configured to: analyze the collected biomass / organic matter on-site, and pretreat the biomass / organic matter accordingly based on the analysis results to obtain at least one of compressed pellets, pyrolytic char, and pyrolytic oil; The new energy power generation module is configured to generate electricity using green energy. The water electrolysis and hydrogen-oxygen storage module is configured to: electrolyze water to generate hydrogen and store hydrogen; The synthesis reaction module is configured to: feed the compressed particles and pyrolysis char pretreated from the pretreatment module into a gasification device for gasification, and react the generated pyrolysis gas with hydrogen generated from water electrolysis to obtain green synthetic fuel; and react the pyrolysis oil pretreated from the pretreatment module with hydrogen generated from water electrolysis under high temperature and high pressure to undergo a hydrogenation and deoxygenation upgrading reaction to obtain green finished oil.

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