Biomass and coal co-pyrolysis reactor

Abstract

The application discloses a biomass and coal co-pyrolysis reactor, which comprises a reactor body, wherein the reactor body comprises a biomass pyrolysis cylinder and a coal pyrolysis cylinder which are communicated with each other, the biomass pyrolysis cylinder is connected below the coal pyrolysis cylinder, the cross-sectional area of the biomass pyrolysis cylinder is smaller than that of the coal pyrolysis cylinder, the bottom of the biomass pyrolysis cylinder is provided with a lifting gas inlet, the gas generated by the coal pyrolysis is suitable to enter the reactor body through the lifting gas inlet, the top of the coal pyrolysis cylinder is provided with a product outlet, at least one biomass feeding port is arranged on the side wall of the biomass pyrolysis cylinder, at least one coal feeding port is arranged on the side wall of the coal pyrolysis cylinder, and a plurality of heat accumulating radiation pipes are arranged in the biomass pyrolysis cylinder and the coal pyrolysis cylinder in a spaced mode. According to the biomass and coal co-pyrolysis reactor, hydrogen in the biomass can be easily transferred to the oil gas in the coal pyrolysis cylinder, and the biomass and the coal pyrolysis can reach a synergistic effect.

Description

Technical Field

[0001] This invention relates to the fields of chemical engineering and energy technology, and in particular to a biomass and coal co-pyrolysis reactor. Background Technology

[0002] Coal is one of the world's most abundant conventional resources with proven reserves. As the world's largest producer and consumer of coal, my country's energy structure is characterized by abundant coal reserves, scarce oil reserves, and limited natural gas. The clean and efficient utilization of coal is an urgent need for national production.

[0003] Meanwhile, my country is also rich in biomass resources. The annual output of just four types of biomass raw materials—crop straw, firewood, animal manure, and household waste—is equivalent to 780 million tons of oil equivalent (TOE), more than 50% of my country's total energy consumption in 2000. As one of the only renewable energy sources that can be stored and transported, biomass has a huge global output, wide distribution, and is less restricted by geographical location; it is also renewable. With increasing global emphasis on energy conservation, environmental protection, and global climate change, renewable energy has become increasingly strategic in energy development, and the conversion of biomass into high-grade gaseous and liquid fuels has attracted significant attention worldwide.

[0004] Compared to coal combustion, gasification, and liquefaction processes, rapid pyrolysis converts coal into solid, liquid, and gaseous products, making it a crucial method for achieving clean coal utilization and an important pathway for converting biomass into liquid fuels and gases. Coal is a hydrogen-poor substance with a low pyrolysis yield. Therefore, external hydrogen gasification is typically used to improve coal conversion rates during pyrolysis. However, the production cost of externally added pure hydrogen is generally high, making the search for an inexpensive hydrogen source a research hotspot. Biomass, as a hydrogen-rich substance, not only has a lower pyrolysis temperature than coal, undergoing pyrolysis before coal, but also produces abundant hydrogen, making it a suitable hydrogen source for coal pyrolysis. It also boasts a high bio-oil yield, although it has a high oxygen content. To overcome the shortcomings of individual pyrolysis of either, co-pyrolysis and gasification of coal and biomass effectively combines their pyrolysis and gasification processes, fully leveraging their advantages, reducing production costs, and increasing the yield of the target product.

[0005] Currently, in terms of heating methods, most existing pyrolysis processes both domestically and internationally employ ceramic balls and semi-coke (a pyrolysis product) as solid heat carriers, or gas from the gasification of semi-coke as a gaseous heat carrier. This heating method involves processes such as heating and separating the heat carrier, resulting in a long system process flow and a high system failure rate. Solid heat carriers such as semi-coke and ceramic balls significantly impact the processing capacity of the pyrolysis furnace, and preheating gaseous heat carriers like coal gas also poses significant safety hazards.

[0006] From the perspective of reactor type, most studies on the co-pyrolysis of biomass and coal employ thermobalance, fixed-bed, fluidized-bed, and entrained-flow reactors. Based on the reactor type, these can be broadly categorized into slow pyrolysis and fast pyrolysis. However, research results rarely indicate a synergistic effect between the two, primarily because the temperature ranges of biomass and coal pyrolysis almost completely overlap, differing by more than 100°C. For slow pyrolysis reactions conducted in thermobalance and fixed-bed reactors, by the time coal begins pyrolysis, the biomass is already largely pyrolyzed, and the excess hydrogen in the biomass cannot be effectively utilized for coal pyrolysis, making a synergistic effect difficult to achieve. For fast pyrolysis conducted in fluidized-bed or entrained-flow reactors, the rapid heating rate reduces the temperature difference between the two pyrolysis reactions, but due to the density difference and airflow effects, the hydrogen-rich biomass is not easily transferred to the coal pyrolysis oil and gas, resulting in a weak synergistic effect. Summary of the Invention

[0007] The present invention aims to at least solve one of the technical problems existing in the prior art. Therefore, one object of the present invention is to provide a biomass and coal co-pyrolysis reactor, which improves the synergistic effect of biomass and coal pyrolysis.

[0008] According to an embodiment of the present invention, a biomass and coal co-pyrolysis reactor includes: a reactor body, the reactor body comprising a biomass pyrolysis cylinder and a coal pyrolysis cylinder that are connected to each other, the biomass pyrolysis cylinder being connected below the coal pyrolysis cylinder, and the cross-sectional area of ​​the biomass pyrolysis cylinder being smaller than the cross-sectional area of ​​the coal pyrolysis cylinder; a lifting gas inlet is provided at the bottom of the biomass pyrolysis cylinder, the gas generated by coal pyrolysis being adapted to enter the reactor body through the lifting gas inlet; a product outlet is provided at the top of the coal pyrolysis cylinder; at least one biomass feed port is provided on the side wall of the biomass pyrolysis cylinder, and at least one coal feed port is provided on the side wall of the coal pyrolysis cylinder; and multiple regenerative radiant tubes are provided at intervals in both the biomass pyrolysis cylinder and the coal pyrolysis cylinder.

[0009] According to embodiments of the present invention, the biomass-coal co-pyrolysis reactor is configured such that the biomass pyrolysis cylinder is connected below the coal pyrolysis cylinder, and the cross-sectional area of ​​the biomass pyrolysis cylinder is smaller than that of the coal pyrolysis cylinder. This allows the hydrogen-rich biomass to be easily transferred to the oil and gas in the coal pyrolysis cylinder, ensuring a synergistic effect between biomass and coal pyrolysis, with a significant synergistic effect. Furthermore, by arranging multiple regenerative radiant tubes at intervals within both the biomass and coal pyrolysis cylinders, compared to traditional heating methods using ceramic balls and pyrolysis product semi-coke as solid heat carriers, or coal gas from semi-coke gasification as gaseous heat carriers, the process is simpler, the system temperature control is more accurate, and temperature adjustment is more convenient. It eliminates the need for heating and separation processes of gaseous and solid heat carriers, reducing the system failure rate. Additionally, by using the gas generated from coal pyrolysis as the lifting gas, there is no need to separate the lifting gas from the pyrolysis products.

[0010] According to some embodiments of the present invention, each of the regenerative radiant tubes is provided with a burner at both ends, and the burners at both ends of each of the regenerative radiant tubes alternately perform combustion.

[0011] According to some embodiments of the present invention, the temperature of the regenerative radiant tube in the biomass pyrolysis cylinder is 350°C to 550°C, and the temperature of the regenerative radiant tube in the coal pyrolysis cylinder is 650°C to 950°C.

[0012] According to some embodiments of the present invention, the temperature difference on each of the heat storage radiant tubes is no higher than 40°C.

[0013] According to some embodiments of the present invention, the distance between the biomass feed inlet and the bottom of the biomass pyrolysis cylinder is 1 / 6 to 1 / 4 of the height of the biomass pyrolysis cylinder; the distance between the coal feed inlet and the bottom of the coal pyrolysis cylinder is 1 / 6 to 1 / 4 of the height of the coal pyrolysis cylinder.

[0014] According to some embodiments of the present invention, the diameter of the biomass pyrolysis cylinder is 20% to 50% of the diameter of the coal pyrolysis cylinder.

[0015] According to some embodiments of the present invention, the height of the biomass pyrolysis cylinder is 30% to 80% of the height of the coal pyrolysis cylinder.

[0016] According to some embodiments of the present invention, the feed flow ratio of the biomass to the coal is between 1:6 and 1:1.

[0017] According to some embodiments of the present invention, a plurality of the regenerative radiant tubes are arranged horizontally at equal intervals in the transverse and longitudinal directions within the reactor body.

[0018] According to some embodiments of the present invention, when the reactor body operates under normal pressure, the cross-sectional shape of the reactor body is square or circular; or when the reactor body operates under high pressure, the cross-sectional shape of the reactor body is circular.

[0019] Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention. Attached Figure Description

[0020] The above and / or additional aspects and advantages of the present invention will become apparent and readily understood from the description of the embodiments taken in conjunction with the following drawings, in which:

[0021] Figure 1 This is a schematic diagram of a biomass and coal co-pyrolysis reactor according to an embodiment of the present invention.

[0022] Figure label:

[0023] 100: Biomass and coal co-pyrolysis reactor;

[0024] 1: Biomass pyrolysis cylinder; 11: Lifting gas inlet; 12: Biomass feed inlet;

[0025] 2: Coal pyrolysis cylinder; 21: Product outlet; 22: Coal feed inlet;

[0026] 3: Thermal storage radiant tube. Detailed Implementation

[0027] The following is for reference. Figure 1 A biomass and coal co-pyrolysis reactor 100 according to an embodiment of the present invention is described.

[0028] like Figure 1 As shown, the biomass and coal co-pyrolysis reactor 100 according to an embodiment of the present invention includes a reactor body.

[0029] Specifically, the reactor body includes a biomass pyrolysis cylinder 1 and a coal pyrolysis cylinder 2 that are interconnected. For example, in Figure 1 In the example, the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 can be arranged coaxially and both extend in the vertical direction, and the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 are internally connected.

[0030] The biomass pyrolysis cylinder 1 has at least one biomass feed port 12 on its side wall, through which biomass such as crop straw, firewood, animal manure, and domestic waste can enter the biomass pyrolysis cylinder 1. The coal pyrolysis cylinder 2 has at least one coal feed port 22 on its side wall, through which coal such as non-caking coal, weakly caking coal, and strongly caking coal can enter the coal pyrolysis cylinder 2.

[0031] Both the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 are equipped with multiple regenerative radiant tubes 3 arranged at intervals. In the description of this invention, "multiple" means two or more. The regenerative radiant tubes 3 provide a heat source for the pyrolysis reaction in the biomass and coal co-pyrolysis reactor 100. When the multiple regenerative radiant tubes 3 are working, the biomass and coal in the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 can be pyrolyzed separately. Moreover, by arranging multiple regenerative radiant tubes 3 at intervals in the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2, a heat source can be provided for the coal and biomass in the reactor body independently. There is no heat carrier or mechanical rotating device, the process flow is simple, the system temperature control is accurate and the temperature adjustment is convenient. There is no need for heating and separation processes of gaseous and solid heat carriers, which reduces the system failure rate. In addition, the biomass and coal can be heated evenly, thereby ensuring the uniform quality of the obtained product and guaranteeing the yield of pyrolysis products. The top of the coal pyrolysis cylinder 2 is provided with a product outlet 21, through which the product obtained after pyrolysis is discharged.

[0032] The biomass pyrolysis cylinder 1 is connected below the coal pyrolysis cylinder 2, and the cross-sectional area of ​​the biomass pyrolysis cylinder 1 is smaller than that of the coal pyrolysis cylinder 2. Therefore, by arranging the biomass pyrolysis cylinder 1 below the coal pyrolysis cylinder 2, the hydrogen-rich material generated during biomass pyrolysis can be easily transferred upwards into the coal pyrolysis cylinder 2 and effectively used for coal pyrolysis within the cylinder, resulting in a significant synergistic effect. Furthermore, by setting the cross-sectional area of ​​the biomass pyrolysis cylinder 1 to be smaller than that of the coal pyrolysis cylinder 2, the synergistic effect between biomass and coal pyrolysis can be effectively ensured. Specifically, for example, because the cross-sectional area of ​​the biomass pyrolysis cylinder 1 is smaller than that of the coal pyrolysis cylinder 2, the hydrogen generated during biomass pyrolysis will first accumulate in the relatively smaller space of the biomass pyrolysis cylinder 1, forming a hydrogen-rich gas. This hydrogen-rich gas will then remain hydrogen-rich when it enters the bottom of the coal pyrolysis cylinder 2.

[0033] The bottom of the biomass pyrolysis cylinder 1 is equipped with a booster gas inlet 11, through which the gas generated from coal pyrolysis enters the reactor body. Thus, by setting the booster gas inlet 11 at the bottom of the biomass pyrolysis cylinder 1 and using the gas generated from coal pyrolysis as the booster gas, the biomass can flow within the biomass pyrolysis cylinder 1 under the action of the booster gas, thereby facilitating the pyrolysis reaction and generating oil and gas. When the oil and gas enter the bottom of the coal pyrolysis cylinder 2 under the action of the booster gas, it provides the necessary hydrogen-rich environment for the coal within the coal pyrolysis cylinder 2, and the coal can flow within the coal pyrolysis cylinder 2 under the action of the booster gas, thereby facilitating the pyrolysis reaction. Moreover, by using the products of coal's own pyrolysis as booster gas to re-participate in the coal pyrolysis process, there is no need to separate them separately.

[0034] Therefore, by integrating biomass pyrolysis and coal pyrolysis into different areas of a single reactor body (i.e., biomass pyrolysis cylinder 1 and coal pyrolysis cylinder 2), and by controlling and increasing the gas flow rate, the residence time of biomass and coal powder is regulated, so that coal pyrolysis is rapidly and completely carried out under the biomass pyrolysis atmosphere, effectively transferring the hydrogen-rich biomass to the coal, thereby improving the coal pyrolysis conversion rate and the yield of the target product.

[0035] According to an embodiment of the present invention, the biomass-coal co-pyrolysis reactor 100, by connecting the biomass pyrolysis cylinder 1 below the coal pyrolysis cylinder 2 and ensuring that the cross-sectional area of ​​the biomass pyrolysis cylinder 1 is smaller than that of the coal pyrolysis cylinder 2, allows the hydrogen-rich biomass to be easily transferred to the oil and gas in the coal pyrolysis cylinder 2, ensuring a synergistic effect between biomass and coal pyrolysis, and this synergistic effect is significant. Furthermore, by arranging multiple regenerative radiant tubes 3 at intervals within the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2, compared to traditional heating methods using ceramic balls and pyrolysis product semi-coke as solid heat carriers, or coal gas from the gasification of semi-coke as a gaseous heat carrier, the process flow is simpler, the system temperature control is more accurate, and temperature adjustment is more convenient. It eliminates the need for heating and separation processes of gaseous and solid heat carriers, reducing the system failure rate. Additionally, by using the gas generated from coal pyrolysis as the lifting gas, there is no need to separate the lifting gas from the pyrolysis products.

[0036] According to some embodiments of the present invention, each regenerative radiant tube 3 is provided with a burner at both ends, and the burners at both ends of each regenerative radiant tube 3 burn alternately. Specifically, for example, the regenerative radiant tube 3 is provided with burners at both ends of its tube body. The flame generated by the burner at one end of the regenerative radiant tube 3 forms a temperature gradient when it is ejected, that is, the temperature gradually decreases from the burner to the outside. Similarly, the flame generated by the burner at the other end of the regenerative radiant tube 3 also forms a temperature gradient when it is ejected. When the burners at both ends of the regenerative radiant tube 3 burn alternately, the two temperature gradients formed are superimposed, thereby making the overall temperature distribution of the entire regenerative radiant tube 3 uniform, and thus ensuring that the reactants in the entire biomass pyrolysis cylinder 1 and coal pyrolysis cylinder 2 are heated uniformly.

[0037] Furthermore, the temperature difference on each regenerative radiant tube 3 is no higher than 40℃. At this point, the difference between the highest and lowest temperatures on each regenerative radiant tube 3 is less than or equal to 40℃. Therefore, if the temperature difference on each regenerative radiant tube 3 is greater than 40℃, the temperature difference on each regenerative radiant tube 3 is relatively large, which may lead to uneven heating of the reactants within the biomass pyrolysis cylinder 1 or the coal pyrolysis cylinder 2. In other words, by setting the temperature difference on each regenerative radiant tube 3 to no higher than 40℃, uniform heating of the reactants within the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 can be effectively guaranteed.

[0038] Optionally, the temperature of the regenerative radiant tube 3 inside the biomass pyrolysis cylinder 1 is 350℃~550℃ (inclusive of the endpoint value), and the temperature of the regenerative radiant tube 3 inside the coal pyrolysis cylinder 2 is 650℃~950℃ (inclusive of the endpoint value). This ensures synergistic effects between biomass and coal pyrolysis. Specifically, a segmented temperature control method is used to reach the optimal temperatures for biomass and coal pyrolysis simultaneously, allowing for the effective transfer of hydrogen-rich substances from the biomass to the coal. This enables complete coal pyrolysis under the biomass pyrolysis atmosphere, thereby improving the coal pyrolysis conversion rate and the yield of the target product.

[0039] According to some embodiments of the present invention, with reference to Figure 1 The biomass feed inlet 12 is located at the lower part of the biomass pyrolysis cylinder 1, and the coal feed inlet 22 is located at the lower part of the coal pyrolysis cylinder 2. Therefore, by arranging the biomass feed inlet 12 at the lower part of the biomass pyrolysis cylinder 1, the biomass can be fully pyrolyzed within the biomass pyrolysis cylinder 1 and then flow upwards into the coal pyrolysis cylinder 2 under the action of the lifting gas, thus ensuring the pyrolysis effect of the biomass and providing a good hydrogen-rich environment for coal pyrolysis. By arranging the coal feed inlet 22 at the lower part of the coal pyrolysis cylinder 2, the newly entering coal from the coal feed inlet 22 can mix better with the oil and gas produced by biomass pyrolysis lifted by the lifting gas below, thus providing the necessary hydrogen-rich environment for coal pyrolysis.

[0040] Further optionally, the distance between the biomass feed port 12 and the bottom of the biomass pyrolysis cylinder 1 is 1 / 6 to 1 / 4 of the height of the biomass pyrolysis cylinder 1 (including the end value), and the distance between the coal feed port 22 and the bottom of the coal pyrolysis cylinder 2 is 1 / 6 to 1 / 4 of the height of the coal pyrolysis cylinder 2 (including the end value).

[0041] Figure 1 The diagram shows two biomass feed ports 12 and two coal feed ports 22 for illustrative purposes. However, those skilled in the art, after reading the following technical solution, will obviously understand that the solution can be applied to a solution with three or more biomass feed ports 12 and coal feed ports 22, which also falls within the protection scope of this invention.

[0042] Specifically, for example, in Figure 1 In the example, a biomass feed port 12 is provided on each side of the biomass pyrolysis cylinder 1, and a coal feed port 22 is provided on each side of the coal pyrolysis cylinder 2. Furthermore, the two biomass feed ports 12 can be opposite each other radially along the biomass pyrolysis cylinder 1, and the two coal feed ports 22 can be opposite each other radially along the coal pyrolysis cylinder 2.

[0043] Optionally, the biomass feed port 12 and the coal feed port 22 are both screw feed ports. In this case, screw feeding mechanisms can be provided at the biomass feed port 12 and the coal feed port 22 respectively, so as to screw-feed the reactants to the corresponding feed ports (i.e., the biomass feed port 12 and the coal feed port 22 mentioned above). However, it is not limited to this.

[0044] The operation process of the biomass and coal co-pyrolysis reactor 100 according to an embodiment of the present invention is as follows:

[0045] Biomass and coal, dried and preheated to a temperature of 100℃~270℃, with 80% of particles smaller than 10mm and 6mm respectively, are fed into the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 through the biomass feed inlet 12 and the coal feed inlet 22, respectively. Lifting gas, generated from coal pyrolysis, is introduced into the lifting gas inlet 11 at the bottom of the biomass pyrolysis cylinder 1. Under the action of the lifting gas, the biomass flows within the biomass pyrolysis cylinder 1 and is heated to 350℃~550℃ within 2~8s by the regenerative radiant tubes 3 inside the biomass pyrolysis cylinder 1, undergoing a pyrolysis reaction to generate oil and gas. This oil and gas, under the action of the lifting gas, enters the bottom of the coal pyrolysis cylinder 2 and mixes with the coal from the coal feed inlet 22 at the bottom of the coal pyrolysis cylinder 2, providing the necessary hydrogen-rich environment for coal pyrolysis. In a hydrogen-rich environment, the coal at the bottom of the coal pyrolysis cylinder 2 flows within the cylinder under the influence of lifting gas. Within 3–10 seconds, it is heated to 650°C–950°C by the radiant tubes, undergoing a pyrolysis reaction to produce gaseous, liquid products and solid semi-coke. These products simultaneously flow upwards along the coal pyrolysis cylinder 2 and exit from the product outlet 21 at the top of the cylinder. From there, they can enter subsequent product dust removal, condensation, separation, and refining systems.

[0046] According to some optional embodiments of the present invention, the diameter of the biomass pyrolysis cylinder 1 is 20% to 50% (including the endpoints) of the diameter of the coal pyrolysis cylinder 2. At this time, the cross-sectional shape of both the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 is circular. Therefore, if the diameter of the biomass pyrolysis cylinder 1 is set to be less than 20% of the diameter of the coal pyrolysis cylinder 2, the small diameter of the biomass pyrolysis cylinder 1 may not be able to provide the required hydrogen-rich environment for coal pyrolysis; if the diameter of the biomass pyrolysis cylinder 1 is set to be greater than 50% of the diameter of the coal pyrolysis cylinder 2, it may not be able to guarantee a good synergistic effect between biomass and coal pyrolysis. In other words, by setting the diameter of the biomass pyrolysis cylinder 1 to be 20% to 50% of the diameter of the coal pyrolysis cylinder 2, while ensuring the provision of the required hydrogen-rich environment for coal pyrolysis, a good synergistic effect between biomass and coal pyrolysis can be effectively guaranteed.

[0047] Furthermore, the height of the biomass pyrolysis cylinder 1 is 30% to 80% of the height of the coal pyrolysis cylinder 2 (including the endpoint values). This further ensures that biomass and coal pyrolysis achieve synergistic effects.

[0048] Optionally, the feed flow ratio of biomass to coal is between 1:6 and 1:1 (inclusive). This further ensures that biomass and coal pyrolysis achieve synergistic effects.

[0049] According to some embodiments of the present invention, such as Figure 1As shown, multiple regenerative radiant tubes 3 are horizontally arranged at equal intervals in both the transverse and longitudinal directions within the reactor body. This further ensures that the biomass and coal within the biomass pyrolysis cylinder 1 and the coal pyrolysis cylinder 2 are heated uniformly.

[0050] In the description of this invention, it should be understood that the terms "center," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "axial," "radial," and "circumferential" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this invention and simplifying the description, and are not intended to indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0051] According to some embodiments of the present invention, when the reactor body operates at atmospheric pressure (i.e., one atmosphere), the cross-sectional shape of the reactor body is square or circular. However, it is not limited to this. It is understood that when the pressure inside the reactor body is approximately the same as the external atmospheric pressure, the specific shape of the reactor body can be designed according to actual needs to better meet practical applications.

[0052] Of course, the present invention is not limited thereto. According to other embodiments of the present invention, when the reactor body operates under high pressure (i.e., greater than one atmosphere), the cross-sectional shape of the reactor body is circular. At this time, since the pressure inside the reactor body is greater than the pressure of the external atmosphere, by setting the cross-sectional shape of the reactor body to be circular, the reactor body can be effectively guaranteed to have good pressure resistance.

[0053] The following example illustrates the process of using rice straw and coal, such as Xuzhou Mining Long Flame Coal, as raw materials. The rice straw is dried to a moisture content of less than 8% and a particle size of less than 8mm, while the Xuzhou Mining Long Flame Coal is dried to a moisture content of less than 15% and a particle size of less than 4mm.

[0054] The feed flow rate of rice straw is 5 kg / s, and the feed flow rate of Xuzhou Coal Mining long-flame coal is 15 kg / s. The rice straw and Xuzhou Coal Mining long-flame coal are added to the biomass feed inlet 12 of biomass pyrolysis cylinder 1 and the coal feed inlet 22 of coal pyrolysis cylinder 2, respectively. Both biomass pyrolysis cylinder 1 and coal pyrolysis cylinder 2 are cylindrical, with diameters of 1 m and 3.5 m, and heights of 3 m and 7.5 m, respectively. The biomass feed inlet 12 is located 0.2 m above the bottom of biomass pyrolysis cylinder 1, and the coal feed inlet 22 is located 0.7 m above the bottom of coal pyrolysis cylinder 2. The reactor body is heated. Within 3-4 seconds, the temperature of the regenerative radiant tube 3 inside biomass pyrolysis cylinder 1 rises to 450-500℃; within 5-6 seconds, the temperature of the regenerative radiant tube 3 inside coal pyrolysis cylinder 2 rises to approximately 800-850℃. The lift gas CH4 enters the bottom of the biomass pyrolysis cylinder 1 through the lift gas inlet 11. Inside the biomass pyrolysis cylinder 1, rice straw undergoes a pyrolysis reaction, producing hydrogen-rich gas. Under the influence of the lift gas CH4, this hydrogen-rich gas rapidly enters the coal pyrolysis cylinder 2 and mixes with the Xuzhou long-flame coal inside, undergoing a pyrolysis reaction to produce pyrolysis gas, tar, water, and semi-coke. These products simultaneously flow upwards along the coal pyrolysis cylinder 2 and exit from the product outlet 21 at the top of the coal pyrolysis cylinder 2, entering the subsequent product dust removal, condensation, separation, and refining system.

[0055] The co-pyrolysis of rice straw and Xuzhou long-flame coal using the above-mentioned biomass and coal co-pyrolysis reactor 100 revealed that the tar yield was on average 40-50% higher than that of the two pyrolysis processes alone, and the conversion rate was 15-25% higher. This indicates that there is a significant synergistic effect between biomass and coal pyrolysis when the biomass and coal co-pyrolysis reactor 100 of the present invention is used.

[0056] The biomass-coal co-pyrolysis reactor 100 according to an embodiment of the present invention is an upward regenerative biomass-coal co-pyrolysis reactor 100, which has the following advantages:

[0057] 1) Integrating biomass pyrolysis and coal pyrolysis into different areas of a single reactor body, by controlling and increasing the gas flow rate and regulating the residence time of biomass and coal powder, the coal pyrolysis is rapidly and completely completed under the biomass pyrolysis atmosphere, effectively transferring the hydrogen-rich biomass to the coal, thereby improving the coal pyrolysis conversion rate and the yield of the target product.

[0058] 2) Multiple regenerative radiant tubes 3 are used to provide heat sources for coal and biomass in the biomass and coal co-pyrolysis reactor 100. There is no heat carrier or mechanical rotating device. The process is simple, the system temperature control is accurate and the temperature adjustment is convenient. There is no need for heating and separation processes of gaseous and solid heat carriers, which reduces the failure rate of the system.

[0059] 3) Combining convection, heat conduction and radiation heat transfer improves the thermal efficiency of the biomass and coal co-pyrolysis reactor 100;

[0060] 4) Compared with semi-coke as a heat carrier, it reduces the dust content of tar;

[0061] 5) It has strong adaptability to various coal types, including non-caking coal, weakly caking coal, and strongly caking coal;

[0062] 6) The biomass and coal co-pyrolysis reactor 100 has a simple structural design, is easy to operate, and is easy to scale up for production.

[0063] In the description of this specification, references to terms such as "one embodiment," "some embodiments," "illustrative embodiment," "example," "specific example," or "some examples," etc., refer to specific features, structures, materials, or characteristics described in connection with that embodiment or example, which are included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example.

[0064] Although embodiments of the invention have been shown and described, those skilled in the art will understand that various changes, modifications, substitutions and alterations can be made to these embodiments without departing from the principles and spirit of the invention, the scope of which is defined by the claims and their equivalents.

Claims

1. A biomass and coal co-pyrolysis reactor, characterized in that, include: The reactor body includes a biomass pyrolysis cylinder and a coal pyrolysis cylinder that are connected to each other. The biomass pyrolysis cylinder is connected below the coal pyrolysis cylinder, and the cross-sectional area of ​​the biomass pyrolysis cylinder is smaller than that of the coal pyrolysis cylinder. The bottom of the biomass pyrolysis cylinder is provided with a lifting gas inlet, through which the gas generated by coal pyrolysis is adapted to enter the reactor body. The top of the coal pyrolysis cylinder is provided with a product outlet. At least one biomass feed port is provided on the side wall of the biomass pyrolysis cylinder, and at least one coal feed port is provided on the side wall of the coal pyrolysis cylinder. Both the biomass pyrolysis cylinder and the coal pyrolysis cylinder are provided with multiple regenerative radiant tubes spaced apart.

2. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, Each of the regenerative radiant tubes is provided with a burner at both ends, and the burners at both ends of each regenerative radiant tube burn alternately.

3. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, The temperature of the regenerative radiant tube inside the biomass pyrolysis cylinder is 350℃~550℃, and the temperature of the regenerative radiant tube inside the coal pyrolysis cylinder is 650℃~950℃.

4. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, The temperature difference on each of the aforementioned heat storage radiant tubes shall not exceed 40°C.

5. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, The distance between the biomass feed inlet and the bottom of the biomass pyrolysis cylinder is 1 / 6 to 1 / 4 of the height of the biomass pyrolysis cylinder; The distance between the coal feed inlet and the bottom of the coal pyrolysis cylinder is 1 / 6 to 1 / 4 of the height of the coal pyrolysis cylinder.

6. The biomass and coal co-pyrolysis reactor according to any one of claims 1-5, characterized in that, The diameter of the biomass pyrolysis cylinder is 20% to 50% of the diameter of the coal pyrolysis cylinder.

7. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, The height of the biomass pyrolysis cylinder is 30% to 80% of the height of the coal pyrolysis cylinder.

8. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, The feed flow ratio of biomass to coal is between 1:6 and 1:

1.

9. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, Multiple regenerative radiant tubes are arranged horizontally at equal intervals in both the transverse and longitudinal directions within the reactor body.

10. The biomass and coal co-pyrolysis reactor according to claim 1, characterized in that, When the reactor body operates under normal pressure, the cross-sectional shape of the reactor body is square or circular; or When the reactor body operates under high pressure, the cross-sectional shape of the reactor body is circular.

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