Biomass direct-combustion coupled wind-light-green-hydrogen carbon dioxide methanol preparation system
The biomass direct combustion coupled with wind, solar and green hydrogen carbon dioxide to methanol system uses CO2 hydrogenation catalyst to synthesize methanol and convert the overhead gas back into carbon dioxide, which solves the problem of high carbon emissions in traditional CO to methanol production and achieves efficient carbon neutrality and resource utilization.
Patent Information
- Application Number
- CN202423307081.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-31
- Publication Date
- 2026-01-23
- Estimated Expiration
- 2034-12-31
AI Technical Summary
Traditional CO-to-methanol production has high carbon emissions, which is not conducive to carbon neutrality. How can we provide a biomass direct combustion coupled with wind, solar and green hydrogen carbon dioxide-to-methanol system to improve the utilization rate of biomass carbon and reduce the carbon waste rate?
A biomass direct combustion coupled with wind, solar and green hydrogen carbon dioxide to methanol system is adopted. Methanol is synthesized using a special CO2 hydrogenation catalyst. The top gas of the crude methanol distillation column is returned to the biomass boiler and converted back into carbon dioxide, improving the utilization rate of biomass carbon. Carbon dioxide storage tanks and hydrogen storage tanks are set up to stabilize the system operation. The heat of reaction is recovered using a lithium bromide unit to produce low-temperature water.
This improved the utilization rate of biomass carbon, reduced the carbon waste rate, ensured that the produced methanol met the European green methanol certification standards, and improved the atom economy and energy utilization efficiency of the system.
Smart Images
Figure CN223818645U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to the technical field of methanol preparation, especially to a carbon dioxide methanol system coupled with biomass direct combustion, wind power and green hydrogen. BACKGROUND
[0002] Carbon neutralization refers to the total amount of carbon dioxide or greenhouse gas emissions directly or indirectly generated within a certain period of time, which is offset by planting trees, energy saving and emission reduction, etc. to offset the carbon dioxide or greenhouse gas emissions generated by itself, so as to realize positive and negative offset. Wind power and solar power electrolysis hydrogen production and methanol production are of great significance to carbon neutralization.
[0003] With the rapid development of renewable energy, the scale of wind power and solar power hydrogen production is huge, and the coupling of CO2 to produce green methanol has become one of the best decarbonization fuels. Biomass is considered as one of the potential green alternative energy sources. Compared with traditional CO methanol, CO2 methanol has higher requirements for catalysts, but traditional CO methanol has high carbon emissions, which is not conducive to carbon neutralization.
[0004] Therefore, how to provide a carbon dioxide methanol system coupled with biomass direct combustion, wind power and green hydrogen to improve the above-mentioned disadvantages is a technical problem that needs to be solved by those skilled in the art at present. UTILITY MODEL CONTENT
[0005] The utility model aims at providing a carbon dioxide methanol system coupled with biomass direct combustion, wind power and green hydrogen, which uses special CO2 hydrogenation catalyst to synthesize methanol, and the overhead gas of the crude methanol rectification tower is returned to the biomass boiler and then converted into carbon dioxide again, thereby improving the utilization rate of biomass carbon and the atomic economy of the system, avoiding resource waste caused by high carbon rejection rate, and ensuring that the prepared methanol meets the European green methanol certification standard.
[0006] To achieve the above-mentioned purpose, the utility model provides a carbon dioxide methanol system coupled with biomass direct combustion, wind power and green hydrogen, which comprises a carbon dioxide production system, a hydrogen production system, a methanol synthesis system and a methanol rectification system. The carbon dioxide production system comprises a biomass boiler for biomass combustion to generate flue gas and a first treatment assembly for treating the flue gas to obtain carbon dioxide. The hydrogen production system can produce hydrogen. The methanol synthesis system comprises a synthesis gas compressor for receiving carbon dioxide and hydrogen to generate synthesis gas, a second treatment assembly connected to the synthesis gas compressor to receive synthesis gas and convert it into a material, and a crude methanol tank connected to the second treatment assembly to receive the material. The methanol rectification system comprises a crude methanol rectification tower connected to the crude methanol tank. The crude methanol rectification tower is provided with a first outlet for methanol discharge and a second outlet for overhead gas discharge. The second outlet is connected to the biomass boiler through a first pipeline.
[0007] Preferably, the methanol rectification system further comprises a fusel oil tank, the crude methanol rectification column is provided with a third outlet for discharging fusel oil product, the third outlet is communicated with an inlet of the fusel oil tank, and an outlet of the fusel oil tank is communicated with the biomass boiler through a second pipeline.
[0008] Preferably, the second processing assembly comprises a high-pressure flash tank and a low-pressure flash tank, an inlet of the low-pressure flash tank is communicated with a first liquid outlet of the high-pressure flash tank, the low-pressure flash tank is used for separation of gas-liquid two-phase fluid, the low-pressure flash tank is provided with a second liquid outlet and a second gas outlet, the second liquid outlet is communicated with an inlet of the crude methanol tank for liquid flow, and the second gas outlet is communicated with the first pipeline for flow of the purge gas to the biomass boiler.
[0009] Preferably, the biomass boiler is provided with a first discharge outlet for discharging flue gas; the first processing assembly comprises:
[0010] a bag-type dust removal device, an inlet of the bag-type dust removal device is communicated with the first discharge outlet, the bag-type dust removal device is provided with a first passage for gas outflow and a second passage for fly ash discharge;
[0011] a carbon dioxide pretreatment device, which is communicated with the first passage;
[0012] a carbon dioxide capture device, which is communicated with an outlet of the carbon dioxide pretreatment device;
[0013] a carbon dioxide post-treatment device, which is communicated with an outlet of the carbon dioxide capture device.
[0014] Preferably, the first processing assembly further comprises:
[0015] a carbon dioxide compressor, which is communicated with the outlet of the carbon dioxide post-treatment device through a third pipeline, and an outlet of the carbon dioxide compressor is communicated with the syngas compressor through a fourth pipeline;
[0016] a carbon dioxide storage tank, which is communicated with the fourth pipeline, and an outlet of the carbon dioxide storage tank is communicated with the third pipeline.
[0017] Preferably, the biomass boiler is provided with a second discharge outlet for discharging steam and a third discharge outlet for discharging ash, the second discharge outlet is communicated with a steam turbine through a first pipeline, and the steam turbine can generate electricity through the steam.
[0018] Preferably, the high-pressure flash tank is further provided with a first gas outlet, and the second processing assembly comprises:
[0019] a recycle gas compressor, which is communicated with the first gas outlet;
[0020] a gas-gas heat exchanger, which is provided with a first tube pass and a first shell pass, an inlet of the first tube pass is communicated with an outlet of the syngas compressor and an outlet of the recycle gas compressor;
[0021] A methanol synthesis tower is connected to the outlet of the first tube pass, and the methanol synthesis tower is provided with a second shell pass, and the second shell pass is provided with a pipeline connected to the synthesis tower steam drum to form a steam-water circulation pipeline, and the outlet of the methanol synthesis tower is connected to the inlet of the first shell pass;
[0022] A lithium bromide unit is connected to the outlet of the first shell pass, and the outlet of the lithium bromide unit is connected to the inlet of the high-pressure flash tank.
[0023] Preferably, the hydrogen production system comprises an electrolytic cell connected with a wind-solar power station and / or a lower power grid through circuit system for electrolyzing water to generate hydrogen and oxygen, the electrolytic cell is provided with a hydrogen outlet for hydrogen discharge and an oxygen outlet for oxygen discharge, the biomass boiler is connected to the oxygen outlet through a second pipeline, and the synthesis gas compressor is connected to the hydrogen outlet through a third pipeline.
[0024] Preferably, the hydrogen production system further comprises:
[0025] A hydrogen storage tank connected to the hydrogen outlet;
[0026] A hydrogen compressor connected to the outlet of the hydrogen storage tank, and the hydrogen compressor is connected to the inlet of the synthesis gas compressor through a fourth pipeline.
[0027] Preferably, the methanol rectification system further comprises:
[0028] A methanol tank connected to the first outlet of the crude methanol rectification tower for collecting refined methanol;
[0029] A loading and unloading platform connected to the outlet of the methanol tank;
[0030] An oil and gas recovery device connected to the exhaust port of the methanol tank and the exhaust port of the loading and unloading platform for oil and gas recovery.
[0031] The carbon dioxide methanol system coupled with biomass direct combustion, wind-solar green hydrogen has at least the following beneficial effects:
[0032] The carbon dioxide preparation system comprises a biomass boiler for biomass combustion to generate flue gas, and a first processing assembly for processing the flue gas to obtain carbon dioxide, a methanol synthesis system for synthesizing crude methanol by using the carbon dioxide and hydrogen prepared by a hydrogen preparation system, only carbon dioxide and hydrogen are used as reaction raw materials, a special CO2 hydrogenation catalyst is used to synthesize methanol, the crude methanol further enters a crude methanol rectification tower of a methanol rectification system to prepare methanol, the crude methanol rectification tower is provided with a first outlet for discharging the methanol and a second outlet for discharging overhead gas, the second outlet is connected to the biomass boiler through a first pipeline, and the first pipeline is used to return the overhead gas of the crude methanol rectification tower to the biomass boiler to be converted into carbon dioxide again, thereby improving the utilization rate of biomass carbon and the atomic economy of the system, avoiding resource waste caused by a high carbon abandonment rate, and ensuring that the prepared methanol meets the European green methanol certification standard. BRIEF DESCRIPTION OF DRAWINGS
[0033] In order to more clearly illustrate the technical solutions in the embodiments of the present application or the prior art, a brief introduction will be given to the drawings needed in the embodiments or prior art description. Obviously, the drawings in the following description are only embodiments of the present application, and other drawings can be obtained by those skilled in the art without creative labor on the basis of the provided drawings.
[0034] Figure 1 The structure schematic diagram of the carbon dioxide methanol preparation system of the biomass direct combustion coupled wind-solar green hydrogen is provided in the embodiments of the present application.
[0035] Among them:
[0036] 1-biomass boiler, 2-bag dust removal device, 3-carbon dioxide pretreatment device, 4-carbon dioxide capture device, 5-carbon dioxide post-treatment device, 6-carbon dioxide compressor, 7-carbon dioxide storage tank, 8-steam turbine, 9-wind-solar power station, 10-electrolytic cell, 11-hydrogen storage tank, 12-hydrogen compressor, 13-syngas compressor, 14-circulating gas compressor, 15-gas-gas heat exchanger, 16-methanol synthesis tower, 17-synthesis tower steam drum, 18-lithium bromide unit, 19-high-pressure flash tank, 20-low-pressure flash tank, 21-crude methanol tank, 22-crude methanol rectification tower, 23-methanol tank, 24-loading and unloading platform, 25-hydrate tank, 26-oil and gas recovery device, 27-first pipeline, 28-second pipeline, 29-third pipeline, 30-fourth pipeline, 31-third pipeline, 32-fourth pipeline, 100-carbon dioxide preparation system, 200-hydrogen preparation system, 300-methanol synthesis system, 400-methanol rectification system. DETAILED DESCRIPTION
[0037] With reference to the drawings of the embodiments of the present application, the technical solutions in the embodiments of the present application will be clearly and completely described, obviously, the described embodiments are only part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments of the present application, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the present application.
[0038] In order for those skilled in the art to better understand the technical solutions of the present application, the present application will be further described in detail below with reference to the drawings and specific embodiments.
[0039] In the description of the present application, it should be understood that the terms "top", "bottom" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the indicated position or element must have a specific orientation, be constructed and operated in a specific orientation, therefore it cannot be understood as a limitation of the present application.
[0040] The purpose of the present application is to provide a kind of biomass direct combustion coupling wind and light green hydrogen's carbon dioxide preparation methanol system, reaction raw material only carbon dioxide and hydrogen, the tower top gas of crude methanol rectification tower 22 is returned to biomass boiler 1 after re-conversion into carbon dioxide, improve the utilization of biomass carbon, improve the atomic economy of system, avoid the resource waste caused by the high carbon rejection rate.
[0041] Please refer to Figure 1 To achieve the above purpose, the present application provides a kind of biomass direct combustion coupling wind and light green hydrogen's carbon dioxide preparation methanol system, including preparation carbon dioxide system 100, preparation hydrogen system 200, methanol synthesis system 300 and methanol rectification system 400, preparation carbon dioxide system 100 includes biomass boiler 1 for biomass combustion to generate flue gas, and the first processing assembly for treating flue gas to obtain carbon dioxide, preparation hydrogen system 200 can prepare hydrogen, methanol synthesis system 300 includes for receiving carbon dioxide and hydrogen to generate synthesis gas synthesis gas compressor 13, is connected to synthesis gas compressor 13 to receive synthesis gas and is converted into material second processing assembly and is connected to the second processing assembly to receive material crude methanol tank 21, methanol rectification system 400 includes the crude methanol rectification tower 22 that is communicated at crude methanol tank 21, crude methanol rectification tower 22 is equipped with first outlet for methanol discharge and second outlet for tower top gas discharge, second outlet is communicated with biomass boiler 1 by first pipeline 27.
[0042] The carbon dioxide preparation system 100 comprises a biomass boiler 1 for biomass combustion to generate flue gas, and a first treatment assembly for treating the flue gas to obtain carbon dioxide, a methanol synthesis system 300 for synthesizing crude methanol by using the carbon dioxide and hydrogen prepared by the hydrogen preparation system 200, and the reaction raw material is only carbon dioxide and hydrogen, a special CO2 hydrogenation catalyst is used to synthesize methanol, and the crude methanol further enters a crude methanol rectification tower 22 of a methanol rectification system 400 to prepare methanol, the crude methanol rectification tower 22 is provided with a first outlet for discharging the methanol and a second outlet for discharging overhead gas, the second outlet is communicated with the biomass boiler 1 through a first pipeline 27, and the first pipeline 27 is used to return the overhead gas of the crude methanol rectification tower 22 to the biomass boiler 1 to be re-converted into carbon dioxide, thereby improving the utilization rate of biomass carbon, improving the atomic economy of the system, avoiding resource waste caused by a high carbon abandonment rate, and ensuring that the prepared methanol meets the European green methanol certification standard.
[0043] In the embodiment, the biomass boiler 1 is provided with a first discharge outlet for discharging flue gas, the biomass boiler 1 is provided with a second discharge outlet for discharging steam and a third discharge outlet for discharging ash, the second discharge outlet is communicated with a steam turbine 8 through a first pipeline, and the steam turbine 8 can generate electricity by using steam; the first treatment assembly comprises a bag dust removal device 2, a carbon dioxide pretreatment device 3, a carbon dioxide capture device 4, a carbon dioxide post-treatment device 5, a carbon dioxide compressor 6 and a carbon dioxide storage tank 7 which are sequentially communicated, specifically, an inlet of the bag dust removal device 2 is communicated with the first discharge outlet, the bag dust removal device 2 is provided with a first channel for discharging gas and a second channel for discharging fly ash; an inlet of the carbon dioxide pretreatment device 3 is communicated with the first channel; an inlet of the carbon dioxide capture device 4 is communicated with an outlet of the carbon dioxide pretreatment device 3; an inlet of the carbon dioxide post-treatment device 5 is communicated with an outlet of the carbon dioxide capture device 4; an inlet of the carbon dioxide compressor 6 is communicated with an outlet of the carbon dioxide post-treatment device 5 through a third pipeline 29, an outlet of the carbon dioxide compressor 6 is communicated with an inlet of a synthesis gas compressor 13 through a fourth pipeline 30; an inlet of the carbon dioxide storage tank 7 is communicated with the fourth pipeline 30, and an outlet of the carbon dioxide storage tank 7 is communicated with the third pipeline 29.
[0044] After pretreatment such as crushing and iron removal, biomass is fed into biomass boiler 1 via a screw feeder and trestle for direct combustion, producing flue gas with a high carbon dioxide content. Simultaneously, high-temperature steam at 540℃ and high pressure at 9.8 MPaG is produced as a byproduct. This high-temperature, high-pressure steam is used to generate electricity for plant use via steam turbine 8. The flue gas from biomass boiler 1 is then processed by bag filter dust collector 2 for dust removal, and by carbon dioxide pretreatment device 3 for removing impurities such as sulfides, nitrogen oxides, and particulate matter. It then enters carbon dioxide capture device 4 for carbon dioxide capture using amine liquid as the capture medium. The desorption temperature is ≤180℃. The desorbed CO2 is then compressed to 1.4 to 1.6 MPaG by carbon dioxide post-treatment device 5 and carbon dioxide compressor 6 before being sent to syngas compressor 13 for further pressure increase. A carbon dioxide storage tank 7 is installed for buffering to reduce the load limitation of the carbon dioxide production system 100, which uses biomass to produce carbon dioxide.
[0045] In this embodiment, the hydrogen production system 200 includes an electrolyzer 10, a hydrogen storage tank 11, and a hydrogen compressor 12. The electrolyzer 10 is connected to a wind and solar power station 9 and / or a power grid via an electrical system for electrolyzing water to generate hydrogen and oxygen. The electrolyzer 10 is provided with a hydrogen outlet for hydrogen discharge and an oxygen outlet for oxygen discharge. The biomass boiler 1 is connected to the oxygen outlet via a second pipe. The inlet of the syngas compressor 13 is connected to the hydrogen outlet via a third pipe 31. The inlet of the hydrogen storage tank 11 is connected to the hydrogen outlet. The inlet of the hydrogen compressor 12 is connected to the outlet of the hydrogen storage tank 11, and the outlet of the hydrogen compressor 12 is connected to the inlet of the syngas compressor 13 via a fourth pipe 32.
[0046] The 220kV green electricity generated by the wind and solar power station 9 is transmitted to the electrolyzer 10 via the circuit system to provide power for hydrogen production through water electrolysis. When necessary, a portion of the grid power can be supplied to maintain the minimum load operation of the electrolyzer 10. Most of the oxygen generated by the electrolyzer 10 is directly discharged into the air, with a reserved portion in the second pipe of the biomass boiler 1 to reduce air consumption. The purified hydrogen has a purity of 99.99% and can be directly used for methanol synthesis. A hydrogen storage tank 11 and a reciprocating hydrogen compressor 12 are installed to adapt to fluctuations in wind power output from the wind and solar power station 9 and reduce the curtailment rate.
[0047] In this embodiment, the second processing component includes a high-pressure flash tank 19 and a low-pressure flash tank 20. The inlet of the low-pressure flash tank 20 is connected to the first liquid outlet of the high-pressure flash tank 19. Both the high-pressure flash tank 19 and the low-pressure flash tank 20 are used for the separation of gas-liquid two-phase fluids. The low-pressure flash tank 20 is provided with a second liquid outlet and a second gas outlet. The second liquid outlet is connected to the inlet of the crude methanol tank 21 to allow liquid to flow into the crude methanol tank 21. The second gas outlet is connected to the first pipeline 27 to allow purge gas to flow into the biomass boiler 1. The high-pressure flash tank 19 is also provided with a first gas outlet. The second processing component also includes a circulating gas compressor 14, a gas-to-gas heat exchanger 15, a methanol synthesis tower 16, and a lithium bromide unit 18. The inlet of compressor 14 is connected to the first gas outlet; gas-gas heat exchanger 15 has a first tube side and a first shell side, the inlet of the first tube side is connected to the outlet of synthesis gas compressor 13 and the outlet of circulating gas compressor 14, that is, the outlet of synthesis gas compressor 13 and the outlet of circulating gas compressor 14 merge and are connected to the inlet of the first tube side; the inlet of methanol synthesis tower 16 is connected to the outlet of the first tube side, methanol synthesis tower 16 has a second shell side, the second shell side has a pipeline connected to the synthesis tower steam drum 17 to form a steam-water circulation pipeline; the outlet of methanol synthesis tower 16 is connected to the inlet of the first shell side; the inlet of lithium bromide unit 18 is connected to the outlet of the first shell side, and the outlet of lithium bromide unit 18 is connected to the inlet of high-pressure flash tank 19.
[0048] CO2 and H2 are mixed in a molar ratio of approximately 1:3 and compressed to 9.0 MPaG by the syngas compressor 13. After heat exchange with the material exiting the methanol synthesis tower 16, the mixture is heated and then enters the methanol synthesis tower 16 for the methanol synthesis reaction. A two-phase water vapor natural circulation stream exists between the second shell side of the methanol synthesis tower 16 and the steam drum of the synthesis tower steam drum 17 to remove the heat of reaction. After depressurization, steam is obtained and can be directed to the steam turbine 8 for power generation within the plant. The material temperature decreases after heat exchange in the gas-to-gas heat exchanger 15. Further heat recovery is achieved in the lithium bromide unit 18, reducing the temperature to 40°C. The 12°C water introduced into the lithium bromide unit 18 is prepared to 7°C water for separation and purification in the electrolyzer 10 and for summer air conditioning in the plant area. After being cooled by the lithium bromide unit 18, the material undergoes gas-liquid separation in the high-pressure flash tank 19. The gas phase with a high H2 content is compressed by the circulating gas compressor 14 and flows into the outlet of the synthesis gas compressor 13, and then re-enters the methanol synthesis tower 16. The liquid phase is processed by the low-pressure flash tank 20 to obtain crude methanol, which is stored in the crude methanol tank 21. The gas phase (purge gas) with a CO2 content of about 60% and an H2 content of about 35% is discharged from the low-pressure flash tank 20 to the first pipeline 27 and then returns to the biomass boiler 1 to recover the carbon source.
[0049] In this embodiment, the methanol distillation system 400 further includes a fusel oil tank 25, a methanol tank 23, a loading / unloading platform 24, and an oil and gas recovery device 26. The crude methanol distillation column 22 is provided with a third outlet for discharging fusel oil products. The third outlet is connected to the inlet of the fusel oil tank 25, that is, the by-products of methanol distillation are connected to the inlet of the fusel oil tank 25. The outlet of the fusel oil tank 25 is connected to the biomass boiler 1 through a second pipeline 28. The inlet of the methanol tank 23 is connected to the first outlet of the crude methanol distillation column 22 for collecting refined methanol. The inlet of loading and unloading platform 24 is connected to the outlet of methanol tank 23; the oil and gas recovery device 26 is connected to the exhaust port of methanol tank 23 and the exhaust port of loading and unloading platform 24 for oil and gas recovery; crude methanol is distilled by crude methanol distillation tower 22 to obtain refined methanol and stored in methanol tank 23; fusel oil and distillation tower top exhaust gas (tower top gas) are recycled to biomass boiler 1; refined methanol is loaded onto trucks as green fuel at loading and unloading platform 24 and sold as a product; methanol-containing tail gas is discharged after methanol is recovered by oil and gas recovery device 26.
[0050] In summary, the biomass direct combustion coupled with wind, solar and green hydrogen carbon dioxide to methanol system provided in this application is equipped with a carbon dioxide storage tank 7 and a hydrogen storage tank 11. The downstream methanol synthesis operation load will not be affected by the wind and solar power output and the adjustment of the biomass boiler 1 by the plant power supply. Biomass direct combustion coupled with wind, solar and green hydrogen to methanol is green and environmentally friendly. The methanol synthesis off-gas, the top gas of the crude methanol distillation tower 22 and the fusel oil by-products are all returned to the biomass boiler 1 to be converted back into carbon dioxide, which improves the utilization rate of biomass carbon and improves the atom economy of the system. The lithium bromide unit 18 fully utilizes the heat of methanol synthesis reaction to produce 7°C low-temperature water, which provides a cold source for the plant air conditioning and water electrolysis to hydrogen purification equipment, improving the energy utilization efficiency of the system.
[0051] It should be noted that in this specification, relational terms such as first and second are used only to distinguish one entity from several other entities, and do not necessarily require or imply any such actual relationship or order between these entities.
[0052] The various embodiments in this specification are described in a progressive manner, with each embodiment focusing on the differences from other embodiments. The same or similar parts between the various embodiments can be referred to each other.
[0053] This article uses specific examples to illustrate the principles and implementation methods of this utility model. The descriptions of the above embodiments are only for the purpose of helping to understand the method and core ideas of this utility model. It should be noted that for those skilled in the art, several improvements and modifications can be made to this utility model without departing from the principles of this utility model, and these improvements and modifications also fall within the protection scope of this utility model.
Claims
1. A biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system, characterized in that, The system includes a carbon dioxide production system (100), a hydrogen production system (200), a methanol synthesis system (300), and a methanol distillation system (400). The carbon dioxide production system (100) includes a biomass boiler (1) for burning biomass to generate flue gas and a first processing component for treating the flue gas to obtain carbon dioxide. The hydrogen production system (200) is capable of producing hydrogen. The methanol synthesis system (300) includes a syngas compressor (13) for receiving carbon dioxide and hydrogen to generate syngas, a second processing component connected to the syngas compressor (13) to receive the syngas and convert it into material, and a crude methanol tank (21) connected to the second processing component to receive the material. The methanol distillation system (400) includes a crude methanol distillation column (22) connected to the crude methanol tank (21). The crude methanol distillation column (22) is provided with a first outlet for methanol discharge and a second outlet for top gas discharge. The second outlet is connected to the biomass boiler (1) through a first pipeline (27).
2. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 1, characterized in that, The methanol distillation system (400) also includes a fusel oil tank (25), the crude methanol distillation column (22) is provided with a third outlet for discharging fusel oil products, the third outlet is connected to the inlet of the fusel oil tank (25), and the outlet of the fusel oil tank (25) is connected to the biomass boiler (1) through a second pipeline (28).
3. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 1, characterized in that, The second processing component includes a high-pressure flash tank (19) and a low-pressure flash tank (20). The inlet of the low-pressure flash tank (20) is connected to the first liquid outlet of the high-pressure flash tank (19). The low-pressure flash tank (20) is used for the separation of gas and liquid two-phase fluids. The low-pressure flash tank (20) is provided with a second liquid outlet and a second gas outlet. The second liquid outlet is connected to the inlet of the crude methanol tank (21) for liquid flow. The second gas outlet is connected to the first pipeline (27) for purge gas to flow to the biomass boiler (1).
4. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 1, characterized in that, The biomass boiler (1) is provided with a first outlet for flue gas discharge; the first processing component includes: The bag filter (2) has an inlet connected to the first outlet, and the bag filter (2) is provided with a first channel for gas outflow and a second channel for fly ash discharge. Carbon dioxide pretreatment device (3) is connected to the first channel; A carbon dioxide capture device (4) is connected to the outlet of the carbon dioxide pretreatment device (3); A carbon dioxide post-treatment device (5) is connected to the outlet of the carbon dioxide capture device (4).
5. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 4, characterized in that, The first processing component further includes: The carbon dioxide compressor (6) is connected to the outlet of the carbon dioxide after-treatment device (5) via a third pipeline (29), and the outlet of the carbon dioxide compressor (6) is connected to the synthesis gas compressor (13) via a fourth pipeline (30). A carbon dioxide storage tank (7) is connected to the fourth pipeline (30), and the outlet of the carbon dioxide storage tank (7) is connected to the third pipeline (29).
6. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 4, characterized in that, The biomass boiler (1) is provided with a second outlet for steam discharge and a third outlet for ash discharge. The second outlet is connected to a steam turbine (8) through a first pipe. The steam turbine (8) is capable of generating electricity through steam.
7. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 3, characterized in that, The high-pressure flash tank (19) is also provided with a first gas outlet, and the second processing component includes: A recirculating gas compressor (14) is connected to the first gas outlet; The gas-to-gas heat exchanger (15) is provided with a first tube side and a first shell side, and the inlet of the first tube side is connected to the outlet of the synthesis gas compressor (13) and the outlet of the circulating gas compressor (14); The methanol synthesis tower (16) is connected to the outlet of the first tube side. The methanol synthesis tower (16) is provided with a second shell side. The second shell side is provided with a pipeline connected to the steam drum (17) of the synthesis tower to form a steam-water circulation pipeline. The outlet of the methanol synthesis tower (16) is connected to the inlet of the first shell side. The lithium bromide unit (18) is connected to the outlet of the first shell side, and the outlet of the lithium bromide unit (18) is connected to the inlet of the high-pressure flash tank (19).
8. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 1, characterized in that, The hydrogen production system (200) includes an electrolyzer (10), which is connected to a wind and solar power station (9) and / or a power grid via an electrical system for electrolyzing water to generate hydrogen and oxygen. The electrolyzer (10) is provided with a hydrogen outlet for hydrogen discharge and an oxygen outlet for oxygen discharge. The biomass boiler (1) is connected to the oxygen outlet via a second pipe, and the syngas compressor (13) is connected to the hydrogen outlet via a third pipe (31).
9. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to claim 8, characterized in that, The hydrogen production system (200) also includes: A hydrogen storage tank (11) is connected to the hydrogen outlet; A hydrogen compressor (12) is connected to the outlet of the hydrogen storage tank (11), and the hydrogen compressor (12) is connected to the inlet of the synthesis gas compressor (13) via a fourth pipe (32).
10. The biomass direct combustion coupled with wind, solar, and green hydrogen carbon dioxide to methanol system according to any one of claims 1-9, characterized in that, The methanol distillation system (400) also includes: A methanol tank (23) is connected to the first outlet of the crude methanol distillation column (22) for the collection of refined methanol; The loading and unloading platform (24) is connected to the outlet of the methanol tank (23); An oil and gas recovery device (26) is connected to the exhaust port of the methanol tank (23) and the exhaust port of the loading and unloading platform (24) for oil and gas recovery.