Co-production system and co-production method for coupling renewable resources with green fuel
Through the co-production system and method, the problems of high carbon emissions and low resource utilization in green methanol production have been solved, efficient utilization of biomass resources and dynamic balance between products have been achieved, and economic benefits and carbon emission effects have been improved.
Patent Information
- Application Number
- CN202510851064.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2025-06-24
- Publication Date
- 2025-09-23
AI Technical Summary
The existing green methanol production process has problems such as high carbon emissions, low biomass resource utilization, single product and difficulty in coping with market fluctuations, and difficulty in absorbing green electricity and green hydrogen, resulting in poor economic benefits and carbon emissions.
A co-production system that couples renewable resources with green fuels is adopted, including a gasification unit, a conversion and heat recovery unit, a desulfurization and decarbonization unit, a cryogenic separation CH4 recovery unit, a synthesis gas compression unit, a biomass methanol synthesis unit, etc. Through biomass gasification and water electrolysis to produce hydrogen, combined with green electricity to produce carbon dioxide capture, the efficient utilization of green hydrogen and green electricity is achieved, and biomass methanol, electronic methanol and SAF are produced.
It has achieved low biomass consumption, on-site consumption of green electricity and green hydrogen, and zero carbon emissions from the device, improved the ability to switch between products and added value, enhanced economic benefits, and achieved the goal of zero CO2 emissions.
Smart Images
Figure CN120682850A_ABST
Abstract
Description
Technical Field
[0001] The present invention belongs to the technical field of biomass chemical production, and in particular relates to a co-production system and method for coupling renewable resources with green fuels. Background Art
[0002] The International Renewable Energy Agency (IRENA) estimates that global methanol CO2 emissions during its lifecycle are approximately 300 million tons per year, accounting for approximately 10% of total CO2 emissions from petrochemical products. This figure is projected to reach 1.5 billion tons per year by 2050. As the world's largest methanol producer and consumer, China accounts for over half of global demand. Therefore, addressing CO2 emissions from methanol production is a critical component of the energy and chemical industry, both globally and domestically.
[0003] Using renewable energy to produce methanol is an effective way to address CO2 emissions from methanol production. There are two pathways for producing methanol from renewable energy: biomass gasification, biomass gasification combined with green hydrogen, and CO2 capture combined with green hydrogen.
[0004] The existing green alcohol production process mainly includes: (1) The process route of bio-green methanol production process is as follows: Figure 1 The bio-green alcohol process is suitable for production in areas with abundant biomass resources. At the same production scale, this solution requires a high biomass demand (approximately 3-4 tons of biomass per ton of methanol) and a complete biomass collection, storage, transportation, and processing chain, particularly requiring high storage space. The yield is approximately 6-8%.
[0005] Its disadvantages are: high carbon emissions, CO2 emissions are 2500-3800Nm 3 / ton of green methanol, the carbon conversion rate of biomass resources is 18% to 25%.
[0006] (2) Biomass gasification + green hydrogen coupled green methanol production process (supporting 200WM wind and solar resources), its production process route is as follows Figure 2 shown.
[0007] The biomass gasification + green hydrogen to green methanol process is suitable for production in areas with scarce biomass resources and good wind and solar resources. Under the same production scale, the biomass demand for green methanol production is reduced by 2.2 to 2.8 tons of biomass per ton of green methanol, but the production capacity is increased by 400 to 500 Nm 3 Green hydrogen / ton of green methanol. The overall yield rate calculated with wind and solar resources is approximately 8-10%.
[0008] Its disadvantages are: CO2 emissions are 800~1000Nm 3 / ton of green methanol, with a carbon conversion rate of 30% to 35%, and a yield rate that lacks competitiveness.
[0009] (3) Electronic methanol production process (350WM new energy), its production process route is as follows Figure 3 shown.
[0010] This production process uses renewable CO2 captured by green electricity such as wind and solar power through water electrolysis to produce hydrogen. Green methanol is produced through mature processes such as compression synthesis and methanol distillation. Its advantages are higher carbon reduction intensity, almost no CO2, nitrogen oxides and particulate matter are produced during the production process, and the impact on the environment is relatively small. The disadvantage is that the green hydrogen consumption is too high (about 2100 Nm 3 Green hydrogen / ton of green methanol. The internal rate of return and the overall rate of return of wind and solar resources are approximately between 1% and 2%.
[0011] When selecting technology routes for renewable resource allocation, such as wind, solar, and agricultural and forestry biomass, green methanol, SAF (sustainable aviation fuel), or green ammonia are options. These options all have certain competitiveness, but in reality, they face the following technical challenges: (1) Green methanol, SAF or green ammonia products are monotonous and lack competitiveness in responding to fluctuations in the green fuel market, making it difficult for economic indicators to achieve ideal results; (2) With a single green methanol or SAF product solution, the carbon utilization rate of biomass is only about 15-30%, resulting in a large amount of carbon source loss and CO2 emissions, and failing to achieve zero carbon emissions; (3) A single product route or unrelated co-production technology makes it difficult to achieve technological transformation between products and optimize the complementary and interconnected regulation of renewable resources; (4) A single product route or unrelated co-production technology can only achieve an overall balance between green electricity and green hydrogen. It is difficult to achieve a dynamic balance between carbon source biomass and downstream synthesis, and it is impossible to achieve flexible load regulation between the chemical side and wind and solar power stations. Summary of the Invention
[0012] Based on the above technical background, the main purpose of the present invention is to provide a co-production system and method of renewable resources coupled with green fuels, which can solve the problems of making full use of the good wind and solar resources in the three northern regions and the southeastern coastal areas under the premise of unchanged biomass raw material consumption, and the difficulties in downstream processes to absorb green hydrogen after green electricity is produced, high long-distance transportation costs, and high carbon emissions of conventional green chemical industries. It achieves the problems of low biomass consumption, on-site absorption of green electricity and green hydrogen, and zero carbon emissions of the device, which not only improves the mutual switching ability between products, but also increases the added value of products, in line with the country's long-term green development policy. At the same time, while achieving a significant improvement in economic benefits from co-production, it can achieve the goal of zero CO2 emissions. To overcome the shortcomings of the existing technology.
[0013] To achieve the aforementioned object of the invention, the technical solutions adopted by the present invention include: The first aspect of the present invention is to provide a co-production system of renewable resources coupled with green fuel, which includes a gasification device, a conversion and heat recovery device, a desulfurization and decarbonization device, a deep cold separation CH4 recovery device, a synthesis gas compression device, a biomass methanol synthesis device and a biomass methanol distillation device.
[0014] The gasification device, the conversion and heat recovery device, the desulfurization and decarbonization device, the deep cold separation CH4 recovery device, the synthesis gas compression device, the biomass methanol synthesis device and the biomass methanol distillation device are connected in sequence.
[0015] The cogeneration system also includes a biomass boiler, a dust removal device, a purification pretreatment device, and a flue gas pressurizing device. The biomass boiler, dust removal device, purification pretreatment device, and flue gas pressurizing device are connected in sequence, and the flue gas pressurizing device is connected to the desulfurization and decarbonization device.
[0016] With this arrangement, the flue gas from the biomass boiler can be transported to the desulfurization and decarbonization device for carbon dioxide capture after dust removal, pretreatment and flue gas pressurization. The remaining tail gas is discharged, and the rich liquid that has absorbed CO2 is transported to the regeneration tower for regeneration to obtain acid gas rich in carbon dioxide, which is then desulfurized and removed from the acid gas to obtain high-purity carbon dioxide.
[0017] According to a preferred embodiment of the present invention, the desulfurization and decarbonization unit includes a first absorption tower, a second absorption tower, and a regeneration tower. The first absorption tower is connected to a conversion and heat recovery unit, and is also connected to a cryogenic separation unit. The carbon monoxide, hydrogen, and methane obtained after desulfurization and decarbonization in the first absorption tower can be transported to a cryogenic separation CH4 recovery unit.
[0018] In the present invention, the absorption tower 1 and the absorption tower 2 may share a regeneration tower, or independently set up regeneration towers according to the scale of the device.
[0019] The second absorption tower is connected to the flue gas booster device. The boosted flue gas is desulfurized and decarbonized by the second absorption tower, and the resulting tail gas is discharged. The rich liquid that has absorbed CO2 is transported to the regeneration tower for regeneration to obtain acidic gas rich in carbon dioxide. The acidic gas is then desulfurized and impurity-removed to obtain high-purity carbon dioxide. After being pressurized by the carbon dioxide compression device, it is gasified for pneumatic transportation and then transported to the first synthesis gas compression device for adjusting the hydrogen-carbon ratio entering the tower for the synthesis of biomass methanol. The remaining majority of carbon dioxide is transported to the second synthesis gas compression device for electronic methanol synthesis.
[0020] The co-production system also includes an acid gas desulfurization device, a carbon dioxide compression device and a second synthesis gas compression device connected in sequence. The acid gas desulfurization device is connected to the regeneration tower in the desulfurization and decarbonization device, the carbon dioxide compression device is connected to both the synthesizer compression device 1 and the synthesis gas compression device 2, and the synthesis gas compression device 2 is also connected to the electronic methanol synthesis device and the electronic methanol purge gas hydrogen recovery device.
[0021] In this arrangement, the acid gas obtained by the desulfurization and decarbonization device is passed into the acid gas desulfurization device for desulfurization, and the obtained carbon dioxide is passed into the carbon dioxide compression device for compression. A small amount of carbon dioxide is passed into the synthesis gas compression device 1, compressed together with hydrogen and carbon monoxide, and then passed into the biomass methanol synthesis device for methanol synthesis.
[0022] The co-production system also includes a water electrolysis hydrogen production device, a hydrogen storage tank and a hydrogen compression device, which are connected in sequence. The hydrogen compression device is connected to the synthesis gas compression device 1, the synthesis gas compression device 2 and the SAF synthesis and refining device.
[0023] The above arrangement allows hydrogen produced by water electrolysis to be stored in a hydrogen storage tank and then passed into a hydrogen compression unit for compression. The first portion of compressed hydrogen is fed into Synthesis Gas Compression Unit 1, where it is transported along with carbon monoxide and hydrogen separated from the cryogenic separation CH4 recovery unit and a portion of carbon dioxide from the CO2 compression unit to the biomass methanol synthesis unit for methanol synthesis. The second portion of compressed hydrogen is fed into Synthesis Gas Compression Unit 2, where it is used together with compressed carbon dioxide from the CO2 compression unit for the synthesis of electronic methanol. The third portion of compressed hydrogen is fed into the SAF synthesis and refining unit to be used as a synthetic and refined feedstock for SAF.
[0024] The co-production system further includes an electronic methanol purge gas hydrogen recovery device, an electronic methanol synthesis device, an electronic methanol distillation device, and a SAF synthesis and refining device. The electronic methanol purge gas hydrogen recovery device, the electronic methanol synthesis device, the electronic methanol distillation device, and the SAF synthesis and refining device are sequentially connected.
[0025] The electronic methanol purge gas hydrogen recovery device is connected to the synthesis gas compression device 2, and the purge gas hydrogen recovery device is also connected to the pipeline between the flue gas purification pretreatment device and the flue gas boosting device.
[0026] With such an arrangement, the purge gas obtained from the electronic methanol synthesis unit can be recovered to the electronic methanol purge gas hydrogen recovery unit. After recovery by the electronic methanol purge gas hydrogen recovery unit, the hydrogen-rich gas is transmitted to the synthesis gas compression unit 2 and used together with compressed carbon dioxide for the synthesis of electronic methanol. The tail gas obtained after the electronic methanol purge gas hydrogen recovery unit recovers the hydrogen-rich gas can be transmitted to the flue gas boosting unit, and the carbon dioxide is captured and recovered through the absorption tower 2, and the inert components are discharged with the tail gas.
[0027] The co-production system described in the present invention can realize the production of biomass methanol by coupling biomass with green hydrogen on a certain scale; at the same time, it can recycle the waste carbon dioxide generated in the production process of biomass methanol and couple it with green hydrogen to produce electronic methanol; and then use green hydrogen to couple electronic methanol to produce green aviation fuel SAF, thereby realizing the co-production of green methanol and SAF, and making the most of tail gas to achieve zero carbon dioxide emissions during the production process.
[0028] The second aspect of the present invention is to provide a method for co-producing renewable resources coupled with green fuels using the co-production system described in the first aspect of the present invention, the co-production method comprising: The medium-pressure superheated steam, biomass particles and oxygen are introduced into the biomass gasification device. After high-temperature gasification, they are introduced into the conversion and heat recovery device for heat recovery. Then it is passed into the absorption tower to absorb sulfide and CO2. The gas after desulfurization and decarbonization enters the deep cold separation CH4 recovery device, part of which obtains green LNG and the other part obtains carbon monoxide and hydrogen.
[0029] The carbon monoxide is introduced into the synthesis gas compression device 1 and compressed together with hydrogen and carbon dioxide. It is then passed into a biomass methanol synthesis unit for synthesis, and finally distilled in a biomass methanol distillation unit to obtain biomass methanol.
[0030] The desulfurization and decarbonization device can absorb and remove sulfur elements in the crude synthesis gas, thereby preventing sulfur elements from entering the synthesis system and causing poisoning and deactivation of the synthesis catalyst.
[0031] Biomass raw materials: refers to the raw materials used in the production and processing of biomass gasifiers using agricultural and forestry waste as raw materials, undergoing an incomplete combustion gasification process to obtain crude synthesis gas of different qualities; Biomass fuel: refers to the production of fuel by biomass boilers using agricultural and forestry waste as raw materials, which are completely burned to produce heat and carbon.
[0032] Biomass pretreatment: This includes crushing, screening, drying, carbonization or molding, and refining to meet the needs of different production processes. Green LNG is a clean energy source and a liquid product made by deep-cooling green methane to -162°C.
[0033] The co-generation method further comprises: The hydrogen produced by electrolysis of water is buffered in a hydrogen storage tank and then compressed and pressurized by a hydrogen compression device. A portion of the compressed hydrogen is then passed into the first synthesis gas compression device to be mixed with carbon monoxide, hydrogen and carbon dioxide produced by biomass gasification for the synthesis of biomass methanol; another portion of the compressed hydrogen is passed into the second synthesis gas compression device to be mixed with carbon dioxide for the synthesis of electronic methanol; the remaining hydrogen is sent to the SAF synthesis and refining device for the SAF production process.
[0034] Green hydrogen refers to hydrogen produced through the electrolysis process using renewable energy sources such as solar or wind power. The present invention uses water electrolysis to produce hydrogen, which can achieve zero carbon emissions.
[0035] Electronic methanol refers to methanol produced by using green electricity obtained from renewable energy sources such as solar energy and wind energy, electrolyzing water to produce green hydrogen, and then capturing and converting the green hydrogen into green carbon dioxide. It is a type of green methanol.
[0036] The co-generation method further comprises: The sulfide and CO2 acid gas obtained in the regeneration tower are passed into the acid gas desulfurization device for desulfurization, and the obtained carbon dioxide is passed into the carbon dioxide compression device for compression, and then passed into the synthesis gas compression device 2 together with the compressed hydrogen obtained from the hydrogen compression device. The synthesis gas compression device 2 also passes the purge gas generated by the methanol synthesis device and the hydrogen-rich gas recovered from the electronic methanol purge gas hydrogen recovery device. The hydrogen-rich gas, purge gas, compressed hydrogen and compressed carbon dioxide in the synthesis gas compression device 2 are compressed together and passed into the electronic methanol synthesis device, and then passed into the electronic methanol distillation device for distillation to obtain electronic methanol, or continue to be passed into the SAF synthesis and refining device to synthesize SAF. The purge gas recovered from the electronic methanol synthesis device is passed into the electronic methanol purge gas hydrogen recovery device for hydrogen recovery. The recovered rich hydrogen is passed into the synthesis gas compression device 2, and the tail gas recovered from the purge gas hydrogen recovery device is passed into the flue gas booster device, and then the carbon dioxide is recovered through the absorption tower 2.
[0037] Purge gas is an inert gas generated during chemical production due to the accumulation of gases that do not participate in the reaction or are too low-grade to be used in chemical equipment or pipelines. The co-generation system and co-generation method of the present invention can fully utilize the effective components of the purge gas.
[0038] SAF has the ability to absorb high-conversion and high-concentration wind, solar and biomass. The product has high added value and low transportation costs. It can be absorbed nearby, which can greatly make up for the limited absorption capacity and high transportation costs of green methanol and green ammonia.
[0039] The present invention uses 650WM (550W wind power, 100W photovoltaic) new energy, green electricity hydrogen production coupled with quantitative biomass gasification to form an annual output of 10wt green methanol, while also being able to co-produce 30,000 tons of SAF. In addition, it can also achieve zero CO2 emissions.
[0040] The cogeneration method of the present invention is based on: 2800 wind power generation hours per year, 1649 photovoltaic power generation hours per year, and the annual power generation is converted to 1.705 billion kWh of electricity. The electricity is generated for self-use, and the grid power is used as a backup power source. A 35t+50t biomass boiler is used as the heat source, with 50t normally open and 35t on standby. The main raw materials for producing 10wt of green methanol by electrolysis of water and coupling with biomass gasification are: about 192,900 tons of biomass pellets and 371 million kWh of green electricity. On this basis, by recycling about 4100Nm2 of biomass gasification emissions, the main raw materials are: about 192,900 tons of biomass pellets and 371 million kWh of green electricity. 3 / h and 4800Nm 3 / h of CO2 and surplus electricity are used to electrolyze water to produce hydrogen, which is coupled to produce about 90,000 tons of electronic methanol, and then through SAF synthesis to form an annual output of 3wt SAF, realizing the joint production of electronic methanol and SAF.
[0041] The co-production method of the present invention is to make full use of new energy green electricity, which meets the green electricity consumption requirements of the current policy trend; at the same time, it does not increase the consumption of biomass raw materials, and produces 3wt / year of SAF products while producing 10wt / year of methanol. The yield rate is increased from 6%-9% of the single yield of 10wt / year green methanol (200wm new energy) to 15%-17%, and CO2 emissions are reduced from 8900Nm 3 / h reduced to 680Nm 3 / h, and zero carbon dioxide emissions can be achieved in chemical production processes.
[0042] For the current renewable resource coupling green fuel project, the present invention proposes a joint production technology solution for wind, solar and agricultural and forestry biomass to produce 100,000 tons of green methanol and 30,000 tons of SAF annually. The joint production method of the present invention can achieve efficient and unified localized consumption of 650MW of wind and solar power and 500,000 tons of agricultural and forestry biomass annually.
[0043] The method adopts the co-production technology of green methanol and SAF, which strengthens the market targeting and can achieve an adjustable product plan with an annual output of 190,000 tons of methanol to 63,000 tons of SAF according to market fluctuations.
[0044] The green methanol and SAF co-production method of the present invention can achieve a timely dynamic balance of green electricity, green hydrogen, green oxygen and green carbon, fully utilize biomass carbon sources, and realize zero carbon emissions.
[0045] The beneficial effects of the present invention are: (1) The co-production system of the present invention utilizes the high conversion, high concentration and high added value of SAF to increase the internal rate of return of a single green methanol project of the same scale from 6-8% to 15-17%; (2) The co-production method of the present invention can achieve dynamic adjustment of the product portfolio from an annual production of 190,000 tons of green methanol to an annual production of 63,000 tons of SAF, thereby enhancing market adaptability; (3) The co-production method described in the present invention can maximize the dynamic balance of green electricity, green hydrogen, green oxygen and green carbon, and achieve efficient utilization of wind, light and biomass coupling to realize quasi-zero carbon emissions; as a co-production technology coupling multiple renewable resources, the present invention not only realizes the efficient on-site consumption of wind, light and agricultural and forestry biomass, but also realizes the optimized combination of products, thereby enhancing the risk resistance of enterprises. BRIEF DESCRIPTION OF THE DRAWINGS
[0046] Figure 1 A flow chart showing the bio-green methanol production process; Figure 2 A flow chart showing the biomass gasification + green hydrogen coupled green methanol production process; Figure 3 A flow chart showing the electronic methanol production process; Figure 4 The process flow chart of the renewable resource coupled green fuel co-production method of the present invention is shown.
[0047] Explanation of Figure Numbers 1-Biomass gasification device; 2-Conversion and heat recovery device; 3- Desulfurization and decarbonization device; 31-Absorption tower 1; 32- Absorption tower 2; 33-Regeneration Tower; 4- Cryogenic separation CH4 recovery device; 5-Synthesis gas compression device 1; 6-Biomass methanol synthesis unit; 7-Biomass methanol distillation unit; 8-Biomass boiler; 9- Boiler flue gas dust removal device; 10-Flue gas purification pretreatment device; 11-Flue gas booster device; 12-Acid gas desulfurization unit; 13- Carbon dioxide compression device; 14-Electrolysis water hydrogen production device; 15-Hydrogen storage tank; 16- Hydrogen compression device; 17-Electronic methanol purge gas hydrogen recovery device; 18-Electronic methanol synthesis unit; 19-Electronic methanol distillation unit; 20-SAF synthesis and purification device; 21-Black ash water treatment device; 22-Synthesis gas compression unit 2. DETAILED DESCRIPTION
[0048] The present invention will be described in detail below, and the characteristics and advantages of the present invention will become clearer and more distinct with the following description.
[0049] Example The present invention is further described below through specific examples. These examples are only intended to illustrate the present invention and are not intended to limit the scope of the present invention.
[0050] Example 1 A co-production system for coupling renewable resources with green fuels, the co-production system comprising a biomass gasification unit 1, a conversion and heat recovery unit 2, a desulfurization and decarbonization unit 3, a cryogenic separation CH4 recovery unit 4, a synthesis gas compression unit 5, a biomass methanol synthesis unit 6, a biomass methanol distillation unit 7, a biomass boiler 8, a boiler flue gas dust removal unit 9, a flue gas purification and pretreatment unit 10, a flue gas pressurizing unit 11, an acid gas desulfurization unit 12, a carbon dioxide compression unit 13, a synthesis gas compression unit 22, a water electrolysis hydrogen production unit 14, a hydrogen storage tank 15, a hydrogen compression unit 16, an electronic methanol purge gas hydrogen recovery unit 17, an electronic methanol synthesis unit 18, an electronic methanol distillation unit 19, a SAF synthesis and refining unit 20, a black ash water treatment unit 21 and a synthesis gas compression unit 22.
[0051] The desulfurization and decarbonization device 3 includes an absorption tower 1 31, an absorption tower 2 32 and a regeneration tower 33. The absorption tower 1 31 is connected to the conversion and heat recovery device 2. The absorption tower 1 31 is also connected to the deep cooling separation CH4 recovery device 4. The absorption tower 2 32 is connected to the flue gas boosting device 11.
[0052] The biomass gasification unit 1, the conversion and heat recovery unit 2, the desulfurization and decarbonization unit 3, the cryogenic separation CH4 recovery unit 4, the synthesis gas compression unit 15, the biomass methanol synthesis unit 6, and the biomass methanol distillation unit 7 are connected in sequence. The biomass boiler 8, the boiler flue gas dust removal unit 9, the flue gas purification and pretreatment unit 10, and the flue gas booster 11 are connected in sequence, and the flue gas booster 11 is connected to the desulfurization and decarbonization unit 3. The acid gas desulfurization unit 12 is connected to the regeneration tower 33 in the desulfurization and decarbonization unit 3. The carbon dioxide compression unit 13 is connected to both the synthesis gas compression unit 15 and the synthesis gas compression unit 22. The synthesis gas compression unit 22 is also connected to the biomass methanol synthesis unit 6 and the electronic methanol purge gas hydrogen recovery unit 17. The water electrolysis hydrogen production unit 14, the hydrogen storage tank 15, and the hydrogen compression unit 16 are connected in sequence, and the hydrogen compression unit 16 is connected to both the synthesis gas compression unit 15 and the synthesis gas compression unit 22. The electronic methanol purge gas hydrogen recovery device 17, the electronic methanol synthesis device 18, the electronic methanol distillation device 19 and the SAF synthesis and refining device 20 are connected in sequence. The purge gas hydrogen recovery device 17 is also connected to the synthesis gas compression device 22, and the electronic methanol purge gas hydrogen recovery device 17 is also connected to the pipeline between the flue gas purification pretreatment device 10 and the flue gas boosting device 11. The black ash water treatment device 21 is connected to the gasification device 1.
[0053] Example 2 A method for co-producing renewable resources and green fuels using the co-production system described in Example 1, the method comprising: Medium-pressure superheated steam, biomass particles and oxygen are introduced into the biomass gasification device 1, and after high-temperature gasification, they are introduced into the conversion and heat recovery device 2 for heat recovery, and then introduced into the absorption tower 31. The gas after desulfurization and decarbonization enters the deep-cold separation CH4 recovery device 4. The first part obtains green LNG, and the other part obtains carbon monoxide, which is introduced into the synthesis gas compression device 5 and co-compressed with green hydrogen and carbon dioxide. Subsequently, it is introduced into the biomass methanol synthesis device 6 to synthesize methanol, and finally distilled into the biomass methanol distillation device 7 to obtain methanol. At the same time, the biomass fuel is introduced into the biomass boiler 8, then dedusted by the boiler flue gas dust removal device 9 and purified by the flue gas purification pretreatment device 10, and then introduced into the flue gas booster 11 for boosting, and then introduced into the absorption tower 2 32. A part of the exhaust gas obtained after absorption is discharged, and the other part is introduced into the deep cold separation CH4 recovery device 4 together with the gas treated from the absorption tower 1 for treatment. The first part obtains green LNG, and the other part obtains carbon monoxide, which is synthesized into methanol with green hydrogen and carbon dioxide.
[0054] At the same time, the electrolysis water hydrogen production device 14 is used to pass the prepared hydrogen into the hydrogen storage tank 15, and then compressed by the hydrogen compression device 16. Subsequently, a part of the compressed hydrogen is passed into the synthesis gas compression device 5, mixed with carbon monoxide, and used for the synthesis of methanol. The other part of the compressed hydrogen is passed into the synthesis gas compression device 22, mixed with carbon dioxide, and used for the synthesis of electronic methanol.
[0055] The acid gas obtained in the regeneration tower 33 is passed into the acid gas desulfurization device 12 for desulfurization, and the obtained carbon dioxide is passed into the carbon dioxide compression device 13 for compression, and then passed together with the compressed hydrogen obtained from the hydrogen compression device 16 into the synthesis gas compression device 22. The synthesis gas compression device 22 also passes the purge gas generated by the biomass methanol synthesis device 6 and the rich hydrogen recovered by the electronic methanol purge gas hydrogen recovery device 17. The rich hydrogen, purge gas, compressed hydrogen and compressed carbon dioxide in the synthesis gas compression device 22 are compressed together. Afterwards, it is passed into the electronic methanol synthesis device 18 to synthesize electronic methanol, and then passed into the electronic methanol distillation device 19 for distillation to obtain electronic methanol, or continues to be passed into the SAF synthesis and refining device 20 to synthesize SAF. The purge gas recovered in the electronic methanol synthesis device 18 is passed into the electronic methanol purge gas hydrogen recovery device 17 for hydrogen recovery, and the recovered hydrogen-rich gas is passed into the synthesis gas compression device 22. The tail gas recovered in the electronic methanol purge gas hydrogen recovery device 17 is passed into the flue gas boosting device 11, and then absorbed by the absorption tower 2 32.
[0056] The present invention is equipped with a gasifier (i.e., gasification device 1), which can produce crude synthesis gas of 31050Nm 3 / h, the gas volume of CO+CO2 reaches 19281.83Nm 3 / h, the synthesis of methanol consumes CO + CO29210 Nm 3 / h, residual CO+CO210071.30 Nm 3 / h, single production of 100,000 tons of green methanol / year, CO2 emissions are 10071.30Nm 3 / h, the present invention can realize the production of 30,000 tons of SAF per year through co-production, and the production of SAF consumes 8725.26 Nm of CO2 3 / h, CO2 emissions are reduced to 1345.74 Nm3 through co-generation 3 / h, the CO2 emission rate is 6.98%, which can basically fully utilize the biomass carbon source and achieve zero CO2 emission.
[0057] The present invention has been described in detail above with reference to specific embodiments and exemplary examples. However, these descriptions should not be construed as limiting the present invention. Those skilled in the art will appreciate that various equivalent substitutions, modifications, or improvements may be made to the technical solutions and implementations of the present invention without departing from the spirit and scope of the present invention, all of which fall within the scope of the present invention. The scope of protection of the present invention shall be determined by the appended claims.
Claims
1. A renewable resource coupled green fuel cogeneration system, characterized in that: The co-generation system includes a biomass gasification device, a conversion and heat recovery device, a desulfurization and decarbonization device, a cryogenic separation CH4 recovery device, a synthesis gas compression device, a biomass methanol synthesis device, a biomass methanol distillation device, a biomass boiler, a boiler flue gas dust removal device, a flue gas purification and pretreatment device, and a flue gas boosting device; The biomass gasification device, the conversion and heat recovery device, the desulfurization and decarbonization device, the cryogenic separation CH4 recovery device, the synthesis gas compression device 1, the biomass methanol synthesis device, and the biomass methanol distillation device are connected in sequence; The biomass boiler, the boiler flue gas dust removal device, the flue gas purification pretreatment device, the flue gas pressurizing device and the desulfurization and decarbonization device are connected in sequence.
2. The renewable resource coupled green fuel cogeneration system according to claim 1, characterized in that: The co-production system also includes a water electrolysis hydrogen production device, a hydrogen storage tank and a hydrogen compression device, which are connected in sequence. The hydrogen compression device is connected to the synthesis gas compression device 1, the synthesis gas compression device 2 and the SAF synthesis and refining device.
3. The renewable resource-coupled green fuel cogeneration system according to claim 1, characterized in that: The co-production system also includes a purge gas hydrogen recovery device, an electronic methanol synthesis device, an electronic methanol distillation device and a SAF synthesis and refining device; the electronic methanol purge gas hydrogen recovery device, the electronic methanol synthesis device, the electronic methanol distillation device and the SAF synthesis and refining device are connected in sequence.
4. The renewable resource coupled green fuel cogeneration system according to claim 1, characterized in that: The desulfurization and decarbonization device includes an absorption tower 1, an absorption tower 2 and a regeneration tower. The absorption tower 1 is connected to a conversion and heat recovery device, and the absorption tower 1 is also connected to a cryogenic separation device. The flue gas boosting device is connected to the second absorption tower device in the desulfurization and decarbonization device.
5. The renewable resource coupled green fuel cogeneration system according to claim 4, characterized in that: The co-generation system also includes an acid gas desulfurization device, a carbon dioxide compression device and a second synthesis gas compression device connected in sequence. The acid gas desulfurization device is connected to the regeneration tower in the desulfurization and decarbonization device, the carbon dioxide compression device is connected to both the synthesizer compression device 1 and the synthesis gas compression device 2, and the synthesis gas compression device 2 is also connected to the electronic methanol synthesis device, the electronic methanol purge gas hydrogen recovery device, and the biomass methanol synthesis device.
6. The renewable resource coupled green fuel cogeneration system according to any one of claims 1 to 5, characterized in that: The electronic methanol purge gas hydrogen recovery device is connected to the synthesis gas compression device 2, and the electronic methanol purge gas hydrogen recovery device is also connected to the pipeline between the flue gas purification pretreatment device and the flue gas boosting device.
7. A method for co-producing renewable resources and green fuels using the renewable resources-coupled green fuel co-production system according to any one of claims 1 to 6, characterized in that: The co-generation method includes: Using recyclable biomass from agricultural and forestry waste as raw materials and steam and oxygen as gasifying agents, crude synthesis gas rich in H2, CO and CH4 is obtained through biomass gasification. After impurity removal, conversion and heat recovery, it is sent to the desulfurization and decarbonization absorption tower 1. The purified gas after CO2 desulfurization and removal is removed and then sent to the deep cold separation CH4 recovery device for removal and recovery of CH4. The by-product is green LNG. After CH4 is removed, the refined synthesis gas rich in CO+H2 is mixed with part of the green hydrogen delivered from the electrolytic water hydrogen production device to meet the hydrogen-carbon ratio requirement of 2.05-2.
15. After being pressurized by the synthesis gas compression device 1, it enters the biomass methanol synthesis device to generate crude methanol under the action of the catalyst, and then transported to the biomass methanol distillation device. After gas-liquid separation and distillation, qualified green methanol products are obtained. The synthesis purge gas is transported to the synthesis gas compression device 2 for recycling.
8. The co-production method according to claim 7, characterized in that: The biomass from agricultural and forestry waste is used as raw material, and air is used as combustion aid to obtain steam through a biomass boiler. The flue gas from the biomass boiler is dusted by a boiler flue gas dust removal device and purified by a flue gas purification pretreatment device, and then passed into a flue gas booster device for boosting. Then it is passed into the absorption tower 2 of the desulfurization and decarbonization device to capture the CO2 in the flue gas, and the remaining tail gas is discharged into the atmosphere. The rich liquid after capturing CO2 is mixed with the rich liquid of the absorption tower 1 in the regeneration tower for regeneration, and regenerated acid gas rich in CO2 and sulfur is obtained at the top of the regeneration tower. High-purity CO2 gas is obtained after desulfurization and impurity removal of the acid gas. After the CO2 gas is pressurized by the carbon dioxide compression device, a small part is returned to the biomass gasification device as a pneumatic conveying gas source, and the other part is sent to the synthesis gas compression device 1 for synthesizing biomass methanol according to the hydrogen-carbon ratio requirement of biomass methanol synthesis. The remaining CO2 gas is sent to the synthesis gas compression device 2 for synthesizing electronic methanol. After mixing with green hydrogen to adjust the hydrogen-carbon ratio to meet the requirements, it is compressed and pressurized by the synthesis gas compression device 2 and sent to the electronic methanol synthesis device. The generated crude methanol is passed through the electronic methanol distillation device to obtain electronic methanol. The electronic methanol purge gas is sent to the electronic methanol purge gas hydrogen recovery device to recover H2 and send the purge gas obtained to the inlet of the biomass boiler flue gas booster device for recycling. The H2 obtained from hydrogen recovery is returned to the inlet of the synthesis gas compression device 2 for recycling.
9. The co-generation method according to claim 8, characterized in that: The green hydrogen produced by wind and solar power generation and water electrolysis is buffered in a hydrogen storage tank and pressurized by a hydrogen compression device. A portion of the H2 at the outlet of the hydrogen compression device is fed into a synthesis gas compression device and mixed with the carbon monoxide and hydrogen produced by biomass gasification and the CO2 output by the carbon dioxide compression device for the synthesis of biomass methanol. Another part of the compressed hydrogen is fed into the synthesis gas compression unit 2 and mixed with carbon dioxide for the synthesis of electronic methanol; The remaining compressed hydrogen is sent to the SAF synthesis and refining unit for the synthesis and refining of SAF.