Biomass dry distillation fluidized bed carbon gas co-production device

Abstract

The invention relates to a biomass dry distillation fluidized bed carbon-gas co-production device, which comprises a solid heat carrier circulating preheating unit, which is used for heating an input low-temperature solid heat carrier into a high-temperature solid heat carrier and outputting the high-temperature solid heat carrier; the biomass dry distillation and carbonization fluidized bed is used for performing carbonization and pyrolysis on the biomass raw material by utilizing the heat of the high-temperature solid heat carrier and the high-temperature pyrolysis gas to form a low-temperature solid heat carrier and a gas-solid mixture containing charcoal; the gas-solid separation unit is used for separating the biochar and high-temperature pyrolysis gas from the gas-solid mixture containing the biochar; the first pyrolysis gas branch is used for being matched with a pyrolysis gas circulating air blower to feed at least part of high-temperature pyrolysis gas of the gas-solid separation unit into a biomass dry distillation carbonization fluidized bed at a first air speed; and the pyrolysis gas dry reforming and heat recovery unit is communicated with the gas-solid separation unit through a second pyrolysis gas branch and is used for carrying out dry reforming on the high-temperature pyrolysis gas and recovering waste heat. The method is suitable for the application field of biomass green energy conversion.

Description

Technical Field

[0001] The invention relates to a biomass dry distillation fluidized bed carbon-gas cogeneration device, which is applicable to the application field of biomass green energy conversion. Background Art

[0002] Green methanol has become the mainstream development direction of future green energy recognized by the world. Moreover, it has been confirmed that the green carbon source required for green methanol synthesis can only be obtained from biomass in a large-scale way.

[0003] At present, the biggest bottleneck facing green methanol production is how to reduce production costs. In the past, people focused on reducing the ways and methods of obtaining biomass. According to the energetic theory: the fixed carbon and volatile carbon contained in biomass should be separated and transformed; from an economic point of view, forestry charcoal making itself is a profitable industry. The pyrolysis gas produced in the charcoal making process can be used if it can be used. If it is not needed, it will be directly burned and discharged. The purpose of direct combustion is only to reduce air pollution.

[0004] At present, biomass will inevitably come into contact with oxygen during the pyrolysis process, which will affect the quality of the generated biochar and thus affect the value of the biochar. Summary of the invention

[0005] The technical problem to be solved by the present invention is: in view of the above-mentioned existing problems, a biomass dry distillation fluidized bed carbon-gas cogeneration device is provided.

[0006] The technical solution adopted by the present invention is: a biomass dry distillation fluidized bed carbon-gas cogeneration device, characterized in that it comprises:

[0007] The solid heat carrier circulation preheating unit is used to heat the input low-temperature solid heat carrier into a high-temperature solid heat carrier and output the high-temperature solid heat carrier;

[0008] A biomass dry distillation carbonization fluidized bed is used to utilize the heat of a high-temperature solid heat carrier and a high-temperature pyrolysis gas to carbonize and pyrolyze the biomass raw material to form a low-temperature solid heat carrier and a gas-solid mixture containing biochar, and output the low-temperature solid heat carrier from a first outlet at the bottom thereof, and output the gas-solid mixture containing biochar from a second outlet at the top thereof;

[0009] A gas-solid separation unit, used for separating biochar and high-temperature pyrolysis gas from a gas-solid mixture containing biochar;

[0010] The first pyrolysis gas branch is used to cooperate with the pyrolysis gas circulation blower to send at least part of the high-temperature pyrolysis gas of the gas-solid separation unit into the biomass dry distillation carbonization fluidized bed at a first wind speed;

[0011] The pyrolysis gas dry reforming and heat recovery unit is connected to the gas-solid separation unit via the second pyrolysis gas branch, and is used to dry reform the high-temperature pyrolysis gas and recover the waste heat;

[0012] The force exerted by the high-temperature pyrolysis gas at the first wind speed on the solid heat carrier in the biomass dry distillation carbonization fluidized bed is smaller than the self-gravity of the solid heat carrier. The high-temperature pyrolysis gas at the first wind speed can drive the gas-solid mixture to be output from the second outlet of the biomass dry distillation carbonization fluidized bed.

[0013] The solid heat carrier circulation preheating unit comprises:

[0014] The solid heat carrier preheating fluidized bed is used to heat the low-temperature solid heat carrier into a high-temperature solid heat carrier through its bottom burner, and its bottom burner is connected to the gas-solid separation unit through a pyrolysis gas third branch equipped with a pyrolysis gas return exhaust fan;

[0015] A solid heat carrier separation collector, used to separate high-temperature solid heat carrier and high-temperature flue gas from the mixture output from the solid heat carrier preheating fluidized bed;

[0016] A high-temperature solid conveyor, used to convey the high-temperature solid heat carrier separated by the solid heat carrier separation collector to the first inlet at the side of the biomass dry distillation carbonization fluidized bed;

[0017] A low-temperature solid return conveyor is used to convey the low-temperature solid heat carrier output from the first outlet at the bottom of the biomass dry distillation carbonization fluidized bed to the side inlet of the solid heat carrier preheating fluidized bed;

[0018] The air separation oxygen generator is connected to the burner at the bottom of the solid heat carrier preheating fluidized bed through the preheating oxygen distribution regulating valve;

[0019] The internal temperature sensor of the preheating fluidized bed is used to collect the internal temperature of the solid heat carrier preheating fluidized bed and is associated with the pyrolysis gas return exhaust fan and the preheating oxygen distribution regulating valve;

[0020] The green carbon dioxide capture unit is connected to the solid heat carrier separation collector via the second flue gas branch, and is used to separate carbon dioxide from the high-temperature flue gas.

[0021] The solid heat carrier circulation preheating unit further includes:

[0022] The first flue gas branch is used to cooperate with the circulating flue gas blower to send at least part of the high-temperature flue gas from the solid heat carrier separation collector into the solid heat carrier preheating fluidized bed bottom burner at a second wind speed;

[0023] The high-temperature flue gas at the second wind speed can drive the solid heat carrier in the solid heat carrier preheating fluidized bed to be output from the top outlet of the solid heat carrier separation collector.

[0024] The second flue gas branch is connected to the solid heat carrier separation collector via a flue gas waste heat boiler.

[0025] The first branch of flue gas is connected to the solid heat carrier separation collector via a flue gas waste heat boiler.

[0026] The green carbon dioxide capture unit includes a front cooling condenser, a carbon dioxide compressor unit, a rear condensing gas-liquid separator and a liquid carbon dioxide storage tank;

[0027] The flue gas passes through the pre-cooling condenser to remove water, then is compressed by the carbon dioxide compressor unit, and then passes through the post-condensation gas-liquid separator to condense the green carbon dioxide and separate it from the non-condensable gas, and then is transported to the liquid carbon dioxide storage tank for storage.

[0028] The green carbon dioxide capture unit also includes an alkaline adsorption column connected to the post-condensation gas-liquid separator for removing acidic gases in non-condensable gases through acid-base neutralization.

[0029] The biomass dry distillation carbonization fluidized bed has:

[0030] The first inlet is located at the side and is used to input high-temperature solid heat carrier;

[0031] The second inlet is located at the side and connected to the biomass feeder for inputting biomass raw materials;

[0032] A third inlet, located at the bottom, for inputting high-temperature pyrolysis gas;

[0033] The first outlet is located at the bottom and is used to output the low-temperature solid heat carrier;

[0034] The second outlet, located at the top, is used to output the gas-solid mixture containing biochar.

[0035] The pyrolysis gas dry reforming and heat recovery unit includes a dry reforming converter and a waste heat steam boiler.

[0036] The solid heat carrier adopts high temperature and wear-resistant inorganic particles to transfer heat to the biomass, so that the biomass can be dry-distilled and pyrolyzed in an anaerobic state, producing high-quality biochar while obtaining high-calorific value bio-pyrolysis gas, which is beneficial to the subsequent purification and energy utilization of the pyrolysis gas.

[0037] The beneficial effects of the present invention are as follows: the present invention heats the solid heat carrier through a solid heat carrier circulation preheating unit, and utilizes the high-temperature solid heat carrier to transfer heat to carbonize and pyrolyze the biomass raw material, so that the biomass does not come into contact with oxygen, and realizes carbonization by dry distillation, and can obtain higher quality biochar, and at the same time obtain pyrolysis gas with higher calorific value, which is beneficial to the back-end energy conversion and utilization of pyrolysis gas. Moreover, in the process of combustion preheating solid heat carrier, flue gas circulation oxygen is used to form oxygen-rich flue gas to assist combustion, which can conveniently realize green carbon dioxide capture and liquefaction. The preheating unit forms a gas-solid mixture containing biochar, and the gas-solid separation obtains biochar and high-temperature pyrolysis gas. The pyrolysis gas is dry reformed to further increase the waste heat temperature, which is more beneficial to the waste heat recovery efficiency. At the same time, the tar gas and methane gas are directly reformed at high temperature to be converted into hydrogen and carbon monoxide, eliminating the trouble of tar gas in the biomass pyrolysis process, purifying the biopyrolysis gas, and facilitating the subsequent clean conversion of green energy.

[0038] The purpose of circulating part of the high-temperature pyrolysis gas to the biomass carbonization fluidized bed in the present invention is to allow the solid heat carrier and biomass to fully flow in the fluidized bed, contact each other, and carbonize quickly. Finally, the carbonized biochar and the generated pyrolysis gas form a gas-solid mixture and are taken out from the second outlet at the top, thereby realizing the separation of the solid heat carrier and the gas-solid mixture through a simple method. The structure is simple, the production is convenient, and the cost is low.

[0039] The present invention continuously replenishes high-temperature solid heat carriers through a first inlet on the side of a biomass dry distillation carbonization fluidized bed, and delivers low-temperature solid heat carriers that have transferred heat to biomass raw materials through a first outlet at the bottom, thereby realizing solid heat carrier circulation, thereby continuously providing sufficient heat for carbonization and pyrolysis of biomass raw materials.

[0040] The solid heat carrier circulation preheating unit in the present invention preheats the pyrolysis gas in the fluidized bed by the solid heat carrier to heat the solid heat carrier, and separates the green carbon dioxide from the flue gas produced by the combustion through the green carbon dioxide capture unit, thereby utilizing the value of the green carbon dioxide to further reduce the production cost of green methanol.

[0041] The present invention can realize large-scale green energy conversion of biomass. At the same time, the production cost of other green energy products can be greatly reduced due to the co-production of biochar. If the biomass raw materials are of good quality and the cost is not high, the output of biochar has high income, plus the carbon sink income, which may offset all the costs in the entire process of production. Other products: heat, electricity, green methanol and green carbon dioxide can achieve partial or full net income. It creates a new situation for the biomass green energy industry to compete with fossil energy in terms of price.

[0042] The present invention adopts pre-air separation oxygen production. The main components of the combustion flue gas are water vapor and green carbon dioxide. Therefore, after removing water and liquefying carbon dioxide, the tail gas emission is directly reduced by more than 90%, simplifying the treatment of tail gas acidic and harmful gases, and achieving both economic and the best emission level since human beings have been involved in combustion. Economically, the cost savings of three main links, such as energy saving by using air separation circulating flue gas to match oxygen to form oxygen-enriched combustion, saving green carbon dioxide separation links and simplifying tail gas purification, can offset the increased power consumption required for oxygen production, making the operating cost more economical than air combustion. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] Figure 1 It is a structural schematic diagram of an embodiment.

[0044] 1. Precooling condenser; 2. Net exhaust flue gas exhaust fan; 2-1. Circulating flue gas blower; 3. Flue gas waste heat boiler; 4. Solid heat carrier preheating fluidized bed; 5. Solid heat carrier separation collector; 6. Biomass feeder; 7. Primary gas-solid separation carbon collector; 8. Secondary gas-solid separation carbon collector; 9. Pyrolysis gas exhaust fan; 10. Burner; 10-1. Spark plug; 11. Dry reforming converter; 12. Waste heat steam boiler; 13. Crude synthesis gas outlet temperature sensor; 14. Dry reforming oxygen regulating valve; 15. Cooling carbon outlet machine; 16, pyrolysis gas circulation blower; 16-1, pyrolysis gas first branch; 17, biomass dry distillation carbonization fluidized bed; 18, high-temperature solid conveyor; 18-1, low-temperature solid return conveyor; 19, pyrolysis gas return exhaust fan; 20, preheating fluidized bed internal temperature sensor; 21, preheating oxygen distribution regulating valve; 22, air separation oxygen generator; 23, circulating flue gas regulating valve; 24, liquid carbon dioxide storage tank; 25, post-condensation gas-liquid separator; 26, alkaline adsorption column; 27, carbon dioxide compression unit; 28, flue gas first branch. DETAILED DESCRIPTION

[0045] like Figure 1 As shown, this embodiment is a biomass dry distillation fluidized bed carbon-gas cogeneration device, which includes a solid heat carrier circulation preheating unit, a biomass dry distillation carbonization fluidized bed, a gas-solid separation unit, and a pyrolysis gas-dry reforming and heat recovery unit.

[0046] In this example, the solid heat carrier circulation preheating unit is used to heat the low-temperature solid heat carrier (using high-temperature resistant and wear-resistant inorganic particles) into a high-temperature solid heat carrier, and has a solid heat carrier preheating fluidized bed, a solid heat carrier separation collector, a flue gas waste heat boiler, a high-temperature solid conveyor, a low-temperature solid return conveyor, an air separation oxygen generator, a preheating fluidized bed internal temperature sensor, a green carbon dioxide capture unit, etc.

[0047] In this example, the solid heat carrier preheating fluidized bed is provided with an inlet on the side, an outlet on the top and a burner on the bottom. The solid heat carrier is input into the solid heat carrier preheating fluidized bed from the side inlet via a low-temperature solid return conveyor, and is heated to a high-temperature solid heat carrier under the action of the burner, and then output from the top outlet as a mixture of the high-temperature solid heat carrier and flue gas generated by combustion.

[0048] In this embodiment, the burner is connected to the gas-solid separation unit via the third pyrolysis gas branch equipped with a pyrolysis gas return exhaust fan, and the pyrolysis gas separated by the gas-solid separation unit is used as the fuel gas; the burner is connected to the air separation oxygen generator via the preheating oxygen distribution regulating valve, and the oxygen output by the air separation oxygen generator is used to assist combustion.

[0049] In this embodiment, the inlet of the solid heat carrier separation collector is connected to the top outlet of the solid heat carrier preheating fluidized bed, and is used to separate high-temperature solid heat carrier and high-temperature flue gas from the mixture output from the solid heat carrier preheating fluidized bed. The high-temperature flue gas is output from the top outlet of the solid heat carrier separation collector, and the high-temperature solid heat carrier freely falls from the bottom outlet of the separation collector into the high-temperature solid conveyor and is sent into the biomass dry distillation carbonization fluidized bed.

[0050] In this example, the inlet of the flue gas waste heat boiler is connected to the top outlet of the solid heat carrier separation collector, which is used to use the high-temperature flue gas to heat soft water to form steam, which can be used for steam power generation; the outlet of the flue gas waste heat boiler is connected to the bottom of the solid heat carrier preheating fluidized bed through the first flue gas branch, and the first flue gas branch is equipped with a circulating flue gas blower and a circulating flue gas regulating valve; the outlet of the flue gas waste heat boiler is connected to the green carbon dioxide capture unit through the second flue gas branch equipped with a net emission flue gas exhaust fan.

[0051] In this embodiment, the temperature sensor inside the preheating fluidized bed is used to collect the temperature inside the solid heat carrier preheating fluidized bed, and is associated with the circulating flue gas regulating valve, the preheating oxygen distribution regulating valve, and the pyrolysis gas return exhaust fan. The control frequency of the circulating flue gas regulating valve, the preheating oxygen distribution regulating valve, the pyrolysis gas return exhaust fan and the temperature sensor inside the preheating fluidized bed form a closed-loop control to ensure that the preheating temperature of the solid heat carrier reaches the temperature requirement of the dry distillation biomass.

[0052] In this embodiment, the first branch of flue gas cooperates with the circulating flue gas blower to send at least part of the high-temperature flue gas of the solid heat carrier separation collector into the bottom burner of the solid heat carrier preheating fluidized bed at the second wind speed. The high-temperature flue gas at the second wind speed can drive a mixture of high-temperature solid heat carrier and flue gas generated by combustion in the solid heat carrier preheating fluidized bed to be output from the top outlet of the solid heat carrier separation collector.

[0053] In this example, the flow rate of the solid heat carrier is controlled by the frequency conversion of the circulating flue gas blower. The blower speed is high, the amount of circulating flue gas entering the preheating fluidized bed is large, and the flow rate of the solid heat carrier brought out is large.

[0054] In this embodiment, the green carbon dioxide capture unit includes a front cooling condenser, a carbon dioxide compressor unit, a rear condensation gas-liquid separator, an alkaline adsorption column and a liquid carbon dioxide storage tank. The flue gas passes through the front cooling condenser to remove water, is compressed by the carbon dioxide compressor unit, and then passes through the rear condensation gas-liquid separator to condense the green carbon dioxide and separate it from the non-condensable gas, and then is transported to the liquid carbon dioxide storage tank for storage and can be taken away at regular intervals.

[0055] In this example, the non-condensable gas separated by the post-condensation gas-liquid separator is rich in acidic gases such as sulfur dioxide, which are removed by acid-base neutralization in the alkaline adsorption column. Finally, the inert gas is directly discharged. Because the amount is small, there is no need to use a chimney, and it can be connected to a ditch or an exhaust port more than one person high.

[0056] In this embodiment, the biomass carbonization fluidized bed has a first inlet and a second inlet located at its side, a third inlet located at its bottom, a first outlet located at its bottom and a second outlet located at its top.

[0057] In this example, the first inlet of the biomass dry distillation carbonization fluidized bed corresponds to a high-temperature solid conveyor, which is used to input high-temperature solid heat carriers into the biomass dry distillation carbonization fluidized bed; the second inlet corresponds to a biomass feeder, which is used to input biomass raw materials into the biomass dry distillation carbonization fluidized bed; the third inlet is connected to the gas-solid separation unit through the first branch of pyrolysis gas of the pyrolysis gas circulation blower, which is used to input the pyrolysis gas separated by the gas-solid separation unit into the biomass dry distillation carbonization fluidized bed.

[0058] In this embodiment, the first branch of the pyrolysis gas cooperates with the pyrolysis gas circulation blower to deliver at least part of the high-temperature pyrolysis gas of the gas-solid separation unit into the biomass dry distillation carbonization fluidized bed at a first wind speed. The high-temperature pyrolysis gas at the first wind speed exerts a force on the solid heat carrier in the biomass dry distillation carbonization fluidized bed that is less than the self-gravity of the solid heat carrier. The high-temperature pyrolysis gas at the first wind speed can drive the gas-solid mixture in the biomass dry distillation carbonization fluidized bed to be output from the second outlet of the biomass dry distillation carbonization fluidized bed.

[0059] In this embodiment, the first outlet of the biomass dry distillation carbonization fluidized bed corresponds to the low-temperature solid return conveyor, which is used to output the low-temperature solid heat carrier in the biomass dry distillation carbonization fluidized bed to the solid heat carrier preheating fluidized bed; the second outlet of the biomass dry distillation carbonization fluidized bed is used to output a gas-solid mixture containing biochar.

[0060] In this example, due to its high density, the solid heat carrier in the biomass carbonization fluidized bed is driven by the pyrolysis gas flow to fully contact and transfer heat with the biomass raw materials input into the fluidized bed. After heat transfer and cold cutting, the solid heat carrier is output from the first outlet and sent back to the solid heat carrier preheating fluidized bed by the low-temperature solid return conveyor for further preheating.

[0061] The biomass raw materials enter the biomass dry distillation carbonization fluidized bed from the biomass feeder. The incoming biomass raw materials need to be pre-crushed into a reasonable particle size. After entering the dry distillation fluidized bed, the biomass raw materials have a large specific gravity and will automatically fall and contact the solid heat carrier. Driven by the high-temperature pyrolysis airflow, the temperature is quickly raised and carbonized and pyrolyzed. After being converted into biochar, the quality of the biochar drops rapidly and is automatically carried upward by the pyrolysis airflow and output from the second outlet of the biomass dry distillation carbonization fluidized bed.

[0062] In this embodiment, the gas-solid separation unit includes a primary gas-solid separation carbon collector, a secondary gas-solid separation carbon collector and a cooling carbon outlet machine. The gas-solid mixture output from the second outlet of the biomass dry distillation carbonization fluidized bed enters the primary gas-solid separation carbon collector to separate biochar and pyrolysis gas. The unseparated biochar continues to enter the secondary gas-solid separation carbon collector. After two stages of gas-solid separation, most of the biochar is collected and dropped into the cooling carbon outlet machine for output.

[0063] In this example, the pyrolysis gas dry reforming and heat recovery unit includes a dry reforming converter and a waste heat steam boiler. The pyrolysis gas is pressurized by a pyrolysis gas exhaust fan and input into a burner in the dry reforming converter. An oxygen conduit connected to an air separation oxygen generator is installed in the burner. A spark plug is placed at the burner mouth, and the flame is ignited and sprayed into the dry reforming converter. The hydrogen in the pyrolysis gas is first burned with oxygen to release heat, and water vapor is generated at the same time. The heat generated heats up the pyrolysis gas to a high temperature, and the high-temperature water vapor, methane gas and tar gas generated undergo reforming endothermic conversion reaction.

[0064] This embodiment performs closed-loop control through the crude synthesis gas outlet temperature sensor at the bottom of the dry reforming converter and the dry reforming oxygen regulating valve. The dry reforming oxygen regulating valve is installed on the oxygen conduit to ensure that the supplied oxygen can meet the heat required for the reforming endothermic reaction and react methane gas and tar gas as completely as possible.

[0065] After leaving the dry reforming converter, the high-temperature crude syngas directly enters the waste heat steam boiler to recover waste heat and generate medium-pressure steam for power generation, thus forming a cascade utilization of energy. The crude syngas leaving the waste heat steam boiler still has a high amount of recoverable waste heat, which can be utilized according to subsequent user needs.

Claims

1. A biomass dry distillation fluidized bed carbon-gas cogeneration device, characterized in that: include: The solid heat carrier circulation preheating unit is used to heat the input low-temperature solid heat carrier into a high-temperature solid heat carrier and output the high-temperature solid heat carrier; The biomass dry distillation carbonization fluidized bed is used to utilize the heat of the high-temperature solid heat carrier to carbonize and pyrolyze the biomass raw materials. The high-temperature pyrolysis gas circulating from the bottom plays a role in full fluidization contact between the biomass and the high-temperature solid heat carrier. The biomass is thermally decomposed to form a low-temperature solid heat carrier and a gas-solid mixed gas flow containing biochar, wherein the low-temperature solid heat carrier is output from the first outlet at the bottom of the fluidized bed, and the gas-solid mixed gas flow is output from the second outlet at the top; A gas-solid separation unit, used for separating biochar and high-temperature pyrolysis gas from a gas-solid mixture containing biochar; The first pyrolysis gas branch is used to cooperate with the pyrolysis gas circulation blower to send at least part of the high-temperature pyrolysis gas of the gas-solid separation unit into the biomass dry distillation carbonization fluidized bed at a first wind speed; The pyrolysis gas dry reforming and heat recovery unit is connected to the gas-solid separation unit via the second pyrolysis gas branch, and is used to dry reform the high-temperature pyrolysis gas and recover the waste heat; The force exerted by the high-temperature pyrolysis gas at the first wind speed on the solid heat carrier in the biomass dry distillation carbonization fluidized bed is smaller than the self-gravity of the solid heat carrier. The high-temperature pyrolysis gas at the first wind speed can drive the gas-solid mixture to be output from the second outlet of the biomass dry distillation carbonization fluidized bed.

2. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 1, characterized in that: The solid heat carrier circulation preheating unit comprises: The solid heat carrier preheating fluidized bed is used to heat the low-temperature solid heat carrier into a high-temperature solid heat carrier through its bottom burner, and its bottom burner is connected to the gas-solid separation unit through a pyrolysis gas third branch equipped with a pyrolysis gas return exhaust fan; A solid heat carrier separation collector, used to separate high-temperature solid heat carrier and high-temperature flue gas from the mixture output from the solid heat carrier preheating fluidized bed; A high-temperature solid conveyor, used to convey the high-temperature solid heat carrier separated by the solid heat carrier separation collector to the first inlet at the side of the biomass dry distillation carbonization fluidized bed; A low-temperature solid return conveyor is used to convey the low-temperature solid heat carrier output from the first outlet at the bottom of the biomass dry distillation carbonization fluidized bed to the side inlet of the solid heat carrier preheating fluidized bed; The air separation oxygen generator is connected to the circulating flue connection inlet pipe on the bottom burner of the solid heat carrier preheating fluidized bed through the preheating oxygen distribution regulating valve, and is configured to produce oxygen-rich flue gas for combustion support; The internal temperature sensor of the preheating fluidized bed is used to collect the internal temperature of the solid heat carrier preheating fluidized bed and is associated with the pyrolysis gas return exhaust fan and the preheating oxygen distribution regulating valve; The green carbon dioxide capture unit is connected to the solid heat carrier separation collector via the second flue gas branch, and is used to separate carbon dioxide from the high-temperature flue gas.

3. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 2, characterized in that: The solid heat carrier circulation preheating unit further includes: The first flue gas branch is used to cooperate with the circulating flue gas blower to send at least part of the high-temperature flue gas from the solid heat carrier separation collector into the solid heat carrier preheating fluidized bed bottom burner at a second wind speed; The high-temperature flue gas at the second wind speed can drive the solid heat carrier in the solid heat carrier preheating fluidized bed to be output from the top outlet of the solid heat carrier separation collector.

4. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 3, characterized in that: The second flue gas branch is connected to the solid heat carrier separation collector via a flue gas waste heat boiler.

5. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 3 or 4, characterized in that: The first flue gas branch is connected to the solid heat carrier separation collector via a flue gas waste heat boiler.

6. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 2, characterized in that: The green carbon dioxide capture unit includes a front cooling condenser, a carbon dioxide compressor unit, a rear condensing gas-liquid separator and a liquid carbon dioxide storage tank; The flue gas passes through the pre-cooling condenser to remove water, then is compressed by the carbon dioxide compressor unit, and then passes through the post-condensation gas-liquid separator to condense the green carbon dioxide and separate it from the non-condensable gas, and then is transported to the liquid carbon dioxide storage tank for storage.

7. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 6, characterized in that: The green carbon dioxide capture unit also includes an alkaline adsorption column connected to the post-condensation gas-liquid separator for removing acidic gases in non-condensable gases through acid-base neutralization.

8. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 1, characterized in that: The biomass dry distillation carbonization fluidized bed has: The first inlet is located at the side and is used to input high-temperature solid heat carrier; The second inlet is located at the side and connected to the biomass feeder for inputting biomass raw materials; A third inlet, located at the bottom, for inputting high-temperature pyrolysis gas; The first outlet is located at the bottom and is used to output the low-temperature solid heat carrier; The second outlet, located at the top, is used to output the gas-solid mixture containing biochar.

9. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 1, characterized in that: The pyrolysis gas dry reforming and heat recovery unit includes a dry reforming converter and a waste heat steam boiler.

10. The biomass dry distillation fluidized bed carbon-gas cogeneration device according to claim 1, characterized in that: The solid heat carrier is made of high temperature resistant and wear resistant inorganic particles.

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