Device and method for preparing carbon-rich fuel gas through biomass gasification based on catalyst in-situ regeneration

Abstract

The invention discloses a device and a method for preparing carbon-rich fuel gas by biomass gasification based on catalyst in-situ regeneration. The device comprises a biomass input unit, a gas input unit and a reaction unit, the biomass input unit is used for adjusting the biomass feeding amount so as to convey biomass to the reaction unit; the gas input unit is used for adjusting the flow of gas and introducing the gas into the reaction unit; the gas comprises air and CO2; the reaction unit sequentially comprises a reforming area, a gasification area and a residue combustion area from top to bottom; biomass is conveyed to the gasification area, air is introduced into the gasification area to react with the biomass to generate combustible gas, solid residues generated after the biomass is gasified fall into the residue combustion area to be combusted, and heat generated by combustion is transferred to the gasification area and the reforming area to provide heat for gasification and reforming. According to the invention, in-situ regeneration of the catalyst and CO production are realized by innovatively utilizing CO2, flexible regulation and control of gas product components are realized, and wide-range adaptability of biomass gasification products in application scenes is effectively improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of biomass gasification, and particularly relates to a device and method for preparing carbon-rich fuel gas based on catalyst in-situ regeneration in biomass gasification. BACKGROUND

[0002] About 9 billion tons of biomass resources such as straw and forestry residues are generated in rural areas of China every year, about 30% of which are open-air burned due to improper treatment, causing serious air pollution. Biomass gasification technology can convert biomass into combustible mixed gas through thermochemical reaction under anoxic or micro-oxygenic condition, realizing resource utilization. After being combined with a fuel gas heat pump, a closed loop of resource on-site conversion and energy on-site consumption is formed. However, the high hydrogen content in the biomass gasification fuel gas may cause unstable combustion, oscillation and even flameout, seriously affecting the safety and efficiency of system operation. The application bottleneck of deep integration of biomass gasification technology and fuel gas heat pump lies in how to realize efficient and stable conversion of biomass raw materials and regulate the carbon-rich and hydrogen-reduced combustible gas components. In the process of regulating the biomass gasification fuel gas components, the catalyst with metal (such as nickel, iron, etc.) as active component is crucial to the product. However, such catalysts generally face severe deactivation problems in long-term high-temperature service. On the one hand, the tar and high molecular hydrocarbons produced in the gasification process are cracked on the surface of the catalyst, and the carbon deposition covers the active sites of the catalyst, resulting in decreased reaction performance; on the other hand, the active metal components sinter, migrate or phase separate in the long-term service, resulting in the destruction of active center structure and the reduction of active center number. These deactivation mechanisms require frequent replacement or regeneration of the catalyst, which not only increases the operation complexity, but also significantly increases the operation cost of the system. SUMMARY

[0003] The present application aims to overcome the shortcomings of the prior art, and provides a device and method for preparing carbon-rich fuel gas based on catalyst in-situ regeneration in biomass gasification, so as to effectively improve the wide-range adaptability of the biomass gasification product in application scenarios and overcome the shortcomings of traditional biomass gasification process, i.e., the catalyst needs to be frequently replaced and regenerated due to carbon deposition and sintering deactivation.

[0004] To achieve the above-mentioned purpose, the technical scheme of the present application is as follows:

[0005] In a first aspect, the present application provides a device for preparing carbon-rich fuel gas based on catalyst in-situ regeneration in biomass gasification, characterized in that the device comprises a biomass input unit, a gas input unit and a reaction unit.

[0006] The biomass input unit is used to adjust the biomass feed quantity, so as to deliver the biomass to the reaction unit.

[0007] The gas input unit is used for adjusting the flow of the gas and introducing the gas into the reaction unit; the gas includes air and CO2;

[0008] The reaction unit includes, from top to bottom, a reforming zone, a gasification zone and a residue combustion zone; the biomass is transported to the gasification zone, air is introduced into the gasification zone to react with the biomass to generate combustible gas, the solid residue generated after the gasification of the biomass falls into the residue combustion zone to be combusted, and the heat generated by the combustion is transferred to the gasification zone and the reforming zone to provide heat for the gasification and the reforming; the reforming zone includes a fuel gas reforming zone and a CO2 reforming zone; the combustible gas generated by the gasification zone is introduced into the fuel gas reforming zone, CO2 is introduced into the CO2 reforming zone, and the combustible gas and CO2 react with oxidized state and reduced state catalysts respectively to generate CO-rich fuel gas and discharge the CO-rich fuel gas from the reaction unit.

[0009] Optionally, the biomass gasification device for producing CO-rich fuel gas based on in-situ catalyst regeneration further includes a gas product collection unit including a negative pressure gas storage tank and connected to the reaction unit, which is used for collecting the CO-rich fuel gas and promoting the flow of the gas in the reaction unit to promote the desorption of the gas reaction process.

[0010] Optionally, the gas input unit includes an electronic flow controller to adjust the flow of air and CO2 by using the electronic flow controller.

[0011] Optionally, the biomass gasification device for producing CO-rich fuel gas based on in-situ catalyst regeneration further includes a gas monitoring unit for monitoring the gas component distribution of the reaction unit in real time to calculate the CO2 conversion rate and the carbon recovery rate and form a control strategy instruction to be transmitted to the electronic flow controller of the gas input unit to regulate the flow of CO2.

[0012] Optionally, the gas monitoring unit includes a gas monitoring point one, a gas monitoring point two and a gas monitoring point three; the gas monitoring point one is arranged at the gas inlet of the fuel gas reforming zone, the gas monitoring point two is arranged at the gas outlet of the CO2 reforming zone, and the gas monitoring point three is arranged at the discharge port of the CO-rich fuel gas.

[0013] Optionally, the carbon recovery rate of the reforming process is calculated by using the gas component data of the gas monitoring point one and the gas monitoring point three; and the CO2 conversion rate is calculated by using the CO2 inlet flow and the gas component data of the gas monitoring point two.

[0014] Optionally, the reforming zone is composed of a honeycomb reactor, and the catalyst active substance of the honeycomb reactor is a composite metal oxide of transition metal and lanthanide metal; the catalyst active substance and the binder are mixed and formed into a honeycomb shape and placed in the honeycomb reactor.

[0015] Optionally, the transition metal and the lanthanide metal are in a ratio range of 1 to 1.2.

[0016] Optionally, the reforming zone further comprises an upper transition zone and a lower transition zone; the honeycomb reactor is driven by the motor to rotate, so that the catalyst circulates through the gas reforming zone, the upper transition zone, the CO2 reforming zone and the lower transition zone.

[0017] In the second aspect, the application provides a method for producing carbon-rich gas by biomass gasification based on in-situ catalyst regeneration, based on the device described above, the method comprises the following steps:

[0018] Air is introduced into the gasification zone, and the gasification zone is heated from room temperature to a gasification temperature by an external heat source, and then biomass is input by a conveying belt, and air is introduced into the gasification zone to react with the biomass;

[0019] The gasification residues generated by gasification enter the residue combustion zone, and the heat generated by combustion is transferred to the reforming zone to provide heat for the reforming of the gasification products;

[0020] The gas products of the gasification zone are introduced into the gas reforming zone, and the gas reacts with the oxidized catalyst to consume H2 with strong reducing activity, while the catalyst is converted into a reduced state; as the honeycomb reactor rotates, the reduced catalyst rotates to the CO2 reforming zone for oxidation regeneration, while CO2 is reduced to produce CO; the carbon recovery rate of the reforming process is calculated by the gas component data of the gas monitoring point one and the gas monitoring point three, and the CO2 conversion rate is calculated by the CO2 inlet flow and the gas component data of the gas monitoring point two;

[0021] If the CO2 conversion rate is < N%, the CO2 flow is controlled to be reduced according to the CO2 conversion rate and the CO2 inlet flow; wherein the CO2 conversion rate calculation formula is X CO2 = (V in- V out ) / V in , wherein V in is the CO2 inlet flow, which is obtained by reading the electronic flow controller of the gas input unit, and V out is the CO2 inlet flow of the gas monitoring point two, which is obtained by reading the test results of the gas chromatograph; the reduction amount of CO2 in the process of controlling the CO2 flow is calculated by the formula V down = (N% - X CO2 ) × V in ;

[0022] If the CO2 conversion rate is ≥ N% and the carbon recovery rate is < M%, the CO2 flow is controlled to be increased according to the carbon recovery rate and the gas flow of the reforming zone inlet; wherein the calculation formula of the carbon recovery rate is wherein V in-co and CO and CO2 flow rates of the gas monitoring point two, The flow rates of various short hydrocarbon gases of the gas monitoring point two are obtained by reading the gas chromatography test results. in-co 、 The flow rates of CO, CO2 and various short hydrocarbon gases of the gas monitoring point three are obtained by reading the gas chromatography test results. The increase amount formula of CO2 flow rate in the process of regulating CO2 flow rate is N and M are natural numbers.

[0023] Compared with the prior art, the present application has the following beneficial effects:

[0024] The present application is based on the demand for carbon-rich and hydrogen-reduced gasification gas in the process of gas demand for gas heat pump in the rural distributed biomass utilization scenario, and innovatively proposes a biomass gasification technology for producing carbon-rich gas based on catalyst in-situ regeneration, which overcomes the shortcomings of traditional biomass gasification process, such as frequent replacement and regeneration caused by catalyst carbon deposition and sintering deactivation, reduces the operation complexity and catalyst replacement cost, and more significantly improves the operation efficiency of the system. At the same time, CO2 is innovatively used to realize catalyst in-situ regeneration and CO production, realize flexible regulation of gas product components, and effectively improve the wide-range adaptability of biomass gasification products in application scenarios. On this basis, based on the CO2 conversion rate, carbon recovery rate and gas component data information of the monitoring point, the regulation flow of the gas input unit in the regulation process is calculated, and catalyst in-situ regeneration and carbon-rich gas regulation are realized. The present application uses a honeycomb reactor to make the catalyst circulate in different reaction zones, and combines the gas component information of the monitoring point to form a control strategy to regulate the gas input flow, realize catalyst in-situ regeneration and carbon-rich gas regulation, and significantly improve the wide-range adaptability and economic benefit of the gasification gas in the gas heat pump system. It can be widely used in the field of biomass resource utilization. BRIEF DESCRIPTION OF DRAWINGS

[0025] Figure 1 The present application provides a principle schematic diagram of a biomass gasification device for producing carbon-rich gas based on catalyst in-situ regeneration;

[0026] Figure 2 The present application provides a structure schematic diagram of a biomass gasification device for producing carbon-rich gas based on catalyst in-situ regeneration;

[0027] Figure 3 The present application provides a bottom structure schematic diagram of a honeycomb reactor;

[0028] Figure 4 The present application provides a top structure schematic diagram of a honeycomb reactor;

[0029] Figure 5 The step flow chart of the method for preparing carbon-rich fuel gas from biomass gasification based on in-situ catalyst regeneration provided by the embodiment of the present application is shown in the figure;

[0030] In the figure: 1, biomass input unit; 11, biomass pulverizer; 2, gas input unit; 21, electronic flow controller; 3, reaction unit; 31, reforming zone; 310, catalyst bed; 311, fuel gas reforming zone, 312, CO2 reforming zone; 313, upper transition zone; 314, lower transition zone; 32, gasification zone; 321, grate conveyor; 33, residual combustion zone; 4, gas product collection unit; 41, negative pressure gas storage tank; 5, gas monitoring unit; 51, gas monitoring point one; 52, gas monitoring point two; 53, gas monitoring point three; 54, central control computer; 55, gas chromatograph; 6, first quartz baffle; 7, opening and closing plate; 8, second quartz baffle; 9, motor; 91, motor transmission shaft; 10, fan-shaped quartz baffle. DETAILED DESCRIPTION

[0031] Embodiment:

[0032] In order to make the above-mentioned purposes, features and advantages of the present application more obvious and easy to understand, the specific embodiments of the present application will be described in detail below in combination with the drawings. In the following description, a large number of specific details are set forth in order to facilitate a full understanding of the present application. However, the present application can be implemented in many other ways different from those described herein, and those skilled in the art can make similar improvements without departing from the connotation of the present application, so the present application is not limited by the specific embodiments disclosed below.

[0033] In the description of the present application, it should be understood that if these terms "center", "longitudinal", "transverse", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential" and the like appear, these terms indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, and are only for the purpose of facilitating the description of the present application and simplifying the description, and are not intended to indicate or imply that the devices or elements referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the present application.

[0034] In addition, if these terms "first", "second" appear, these terms are only for the purpose of description, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the technical features indicated. Therefore, the features limited by "first" and "second" can explicitly or implicitly include at least one of the features. In the description of the present application, if the term "multiple" appears, the meaning of "multiple" is at least two, such as two, three, etc., unless otherwise specifically limited.

[0035] In the present application, unless specifically defined otherwise, if there are terms such as "mount", "connect", "connect", "fix" and the like, these terms should be interpreted in a broad sense. For example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be mechanically connected, or it can be electrically connected; it can be directly connected, or it can be indirectly connected through an intermediate medium; it can be the internal communication of two elements or the interaction relationship between two elements, unless otherwise specifically defined. For those skilled in the art, the above terms can be understood in the context of the present application according to the specific circumstances.

[0036] In the present application, unless specifically defined otherwise, if there are terms such as "first feature on the second feature" or "below" and the like, it can mean that the first and second features are in direct contact, or the first and second features are indirectly in contact through an intermediate medium. Moreover, the first feature "above", "above" and "above" of the second feature can be the first feature directly above or obliquely above the second feature, or it can only mean that the first feature is higher than the second feature in horizontal height. The first feature "below", "below" and "below" of the second feature can be the first feature directly below or obliquely below the second feature, or it can only mean that the first feature is lower than the second feature in horizontal height.

[0037] It should be noted that if an element is referred to as "fixed to" or "provided on" another element, it can be directly on another element or there can be a middle element. If an element is considered to be "connected" to another element, it can be directly connected to another element or there can be a middle element. If there is, the terms "vertical", "horizontal", "up", "down", "left", "right" and the like used in the present application are for illustrative purposes only, and are not the only embodiment.

[0038] Referring to Figures 1-2 As shown in the embodiment, the device for preparing carbon-rich gas based on catalyst in-situ regeneration provided by the embodiment mainly comprises a biomass input unit 1, a gas input unit 2 and a reaction unit 3.

[0039] The biomass input unit 1 is equipped with a biomass crusher 11 for crushing biomass and adjusting the biomass feed amount, and the biomass is conveyed to the reaction unit 3 by a conveyor belt

[0040] The gas input unit 2 is used to adjust the flow of gas and introduce it into the reaction unit 3; the gas includes air, CO2 and argon;

[0041] The reaction unit 3 includes, from top to bottom, a reforming zone 31, a gasification zone 32, and a residue combustion zone 33; the biomass is transported to the gasification zone 32, air is introduced into the gasification zone 32 to react with the biomass to generate combustible gas (H2, CO, C n H m ); air and argon are introduced into the residue combustion zone 33, and the solid residue generated after gasification of the biomass falls into the residue combustion zone 33 for combustion, and the heat generated by the combustion is transferred to the gasification zone 32 and the reforming zone 31 to provide heat for gasification and reforming; the reforming zone 31 includes a fuel gas reforming zone 311 and a CO2 reforming zone 312; the combustible gas generated by the gasification zone 32 is introduced into the fuel gas reforming zone 311, and CO2 is introduced into the CO2 reforming zone 312, and the combustible gas and CO2 react with oxidized and reduced catalysts, respectively, to generate CO-rich fuel gas and discharge the reaction unit 3. In addition, the outside of the reforming zone 31 and the gasification zone 32 is a heater to adjust the reaction temperature in the reforming zone 31 and the gasification zone 32.

[0042] Therefore, the device innovatively uses CO2 to achieve in-situ regeneration of the catalyst and production of CO, flexibly regulates the components of the gas product, effectively improves the wide-range adaptability of the biomass gasification product in application scenarios, overcomes the shortcomings of traditional biomass gasification processes that require frequent replacement and regeneration due to catalyst coking and sintering deactivation, reduces the complexity of operation and the cost of catalyst replacement, and more significantly improves the operating efficiency of the system.

[0043] In a preferred embodiment, the biomass gasification device for producing CO-rich fuel gas based on in-situ regeneration of the catalyst further includes a gas product collection unit 4, which includes a negative pressure gas storage tank 41 connected to the CO-rich fuel gas discharge port of the reaction unit 3, for collecting CO-rich fuel gas and promoting gas flow in the reaction unit 3 to facilitate desorption of the gas reaction process.

[0044] In a specific embodiment, the gas input unit 2 includes an electronic flow controller 21 to adjust the flow of air and CO2 using the electronic flow controller 21, and by regulating the CO2 flow that affects the gasification performance, in-situ regeneration of the catalyst and carbon-rich regulation of the gasification fuel gas are achieved.

[0045] In a preferred embodiment, the biomass gasification device for producing CO-rich fuel gas based on in-situ regeneration of the catalyst further includes a gas monitoring unit 5 for real-time monitoring of the gas component distribution of the reaction unit 3, and then transmitting the detection results to the central computer 54 of the gas monitoring unit 5 to calculate the CO2 conversion rate and carbon recovery rate, and form a control strategy instruction to be transmitted to the electronic flow controller 21 of the gas input unit 2 for regulation of the CO2 flow. In this way, by combining the carbon-containing components (such as CO, CO2, and C n H m) analysis and evaluation, CO2 flow affecting gasification performance is regulated, realizing catalyst in-situ regeneration and carbon-rich gas regulation. When CO2 conversion rate is too low, CO2 flow can be reduced; when CO2 conversion rate is high and carbon recovery rate is low, CO2 flow can be increased. It is especially suitable for rural distributed biomass gasification coupled with gas heat pump application scenarios.

[0046] Specifically, the gas monitoring unit 5 includes gas monitoring point one 51, gas monitoring point two 52, and gas monitoring point three 53; the gas monitoring point one 51 is arranged at the gas inlet of the gas reforming zone 311, the gas monitoring point two 52 is arranged at the gas outlet of the CO2 reforming zone 312, and the gas monitoring point three 53 is arranged at the discharge port of the CO-rich gas (i.e. the inlet of the gas product collection unit). In this way, by ingeniously designing three gas monitoring points, detecting the gas components in three different regions through the gas chromatograph 55, calculating the carbon recovery rate of the reforming process through the gas components data of the gas monitoring point one and the gas monitoring point three, and calculating the CO2 conversion rate through the CO2 inlet flow and the gas component data of the gas monitoring point two, the carbon recovery rate of the reforming process is calculated as the feedback signal of the gas input unit to regulate the gas input flow of the reforming zone.

[0047] In a specific embodiment, a first quartz baffle 6 is arranged in the gasification zone 32, the first quartz baffle 6 is fixedly connected with the inner wall of the gasification zone 32, the first quartz baffle 6 includes a horizontal part and an inclined part, a grate conveyor belt 321 is arranged above the horizontal part, and the side connected with the inclined part is provided with an opening and closing plate 7, which sends the gasification residues into the residue combustion zone 33 when the opening and closing plate 7 is opened. The argon inlet of the residue combustion zone 33 is arranged to pass argon at a set angle to the first quartz baffle 6, and the air in the gasification residue combustion zone 33 is blocked from entering the gasification zone 32 when the opening and closing plate 7 is opened.

[0048] In a specific embodiment, as shown in FIG. 6, the gasification zone 32 is provided with a first quartz baffle 6, the first quartz baffle 6 is fixedly connected with the inner wall of the gasification zone 32, the first quartz baffle 6 includes a horizontal part and an inclined part, a grate conveyor belt 321 is arranged above the horizontal part, and the side connected with the inclined part is provided with an opening and closing plate 7, which sends the gasification residues into the residue combustion zone 33 when the opening and closing plate 7 is opened. The argon inlet of the residue combustion zone 33 is arranged to pass argon at a set angle to the first quartz baffle 6, and the air in the gasification residue combustion zone 33 is blocked from entering the gasification zone 32 when the opening and closing plate 7 is opened. Figures 3-4As shown, the reforming zone 31 is composed of a honeycomb reactor, the bottom of which is provided with a sieve plate for placing the shaped oxygen carrier, and the bottom is fixed to the inner wall of the device by a second quartz baffle 8, which is separated into a gas reforming zone 311, an upper transition zone 313, a CO2 reforming zone 312, and a lower transition zone 314. The CO2 reforming zone 312 constitutes a gas inlet area that blocks the reforming medium CO2 from entering the gasification zone 32. The top of the reactor is fixed to the inner wall by a fan-shaped quartz baffle 10, which constitutes a CO2 reforming gas outlet area that blocks the gas from the gas reforming gas outlet from entering the monitoring point two 52. In addition, the reforming zone also contains a motor 9, which drives the honeycomb reactor to rotate through a motor transmission shaft 91, so that the catalyst circulates through the gas reforming zone 311, the upper transition zone 313, the CO2 reforming zone 312, and the lower transition zone 314. The main active substance of the catalyst of the honeycomb reactor is a composite metal oxide of transition metals and lanthanide metals, and the optimal ratio of transition metals to lanthanide metals is 1-1.2. The active substance (composite metal oxide) of the catalyst and the binder are mixed and formed into a honeycomb shape to increase the contact area, and are placed in the honeycomb reactor to form a catalyst bed layer 310.

[0049] Correspondingly, referring to Figure 5 As shown, the embodiment also provides a method for producing carbon-rich gas by biomass gasification based on in-situ catalyst regeneration. Based on the device described above, the method comprises the following steps:

[0050] S1: air is introduced into the gasification zone, the gasification zone is heated from room temperature to a gasification temperature by an external heat source, then biomass is input through a conveyor belt, and the air is introduced into the gasification zone to react with the biomass;

[0051] S2: the gasification residues generated by gasification enter the residue combustion zone, and the heat generated by combustion is transferred to the reforming zone to provide heat for the reforming of the gasification products.

[0052] S3: the gas products of the gasification zone are introduced into the gas reforming area through the fan-shaped gap, the gas reacts with the oxidized catalyst to consume H2 with strong reduction activity, and at the same time, the catalyst is converted into a reduced state. With the rotation of the honeycomb reactor, the reduced catalyst rotates to the CO2 reforming zone for oxidation regeneration, and at the same time, CO is generated by reducing CO2. The carbon recovery rate in the reforming process is calculated by the gas component data of the gas monitoring point one and the gas monitoring point three, and the CO2 conversion rate is calculated by the CO2 inlet flow and the gas component data of the gas monitoring point two;

[0053] S4: if the CO2 conversion rate is <90%, the flow of CO2 is controlled to be reduced according to the CO2 conversion rate and the CO2 inlet flow. The CO2 conversion rate calculation formula is X CO2 = (V in- V out ) / V in , wherein V inV is the CO2 inlet flow rate, obtained by reading the gas input unit electronic flow controller, V out V is the CO2 inlet flow rate of gas monitoring point two, obtained by reading the gas chromatography test results. The calculation formula of the CO2 reduction amount during the CO2 flow regulation process is V down = (90% - X CO2 ) x V in ;

[0054] S5: If the CO2 conversion rate is ≥ 90% and the carbon recovery rate is < 95%, increase the CO2 flow rate according to the carbon recovery rate and the gas flow rate at the inlet of the reforming zone. The calculation formula of the carbon recovery rate is V and V in-co are the CO and CO2 inlet flow rates of gas monitoring point two, V is the flow rate of each type of short hydrocarbon gas at gas monitoring point two, obtained by reading the gas chromatography test results. Similarly, V in-co , and are the CO, CO2 and each type of short hydrocarbon gas flow rates at gas monitoring point three, obtained by reading the gas chromatography test results. The increase amount formula of CO2 during the CO2 flow regulation process is

[0055] In summary, the method of the present embodiment has the following beneficial effects compared to the prior art:

[0056] (1) Catalyst stability: The use of a composite metal oxide with a transition metal and a lanthanide metal ratio range of 1-1.2 as a catalyst is proposed, which realizes in-situ regeneration of the catalyst through oxygen release and oxygenation cycles, overcoming the need for frequent replacement and regeneration of the catalyst due to catalyst carbon deposition and sintering deactivation in traditional biomass gasification processes, reducing the complexity of operation and the cost of catalyst replacement, and more significantly improving the operating efficiency of the system.

[0057] (2) Carbon-rich gas component regulation: The use of CO2 to realize in-situ regeneration of the catalyst and CO production is innovative, which realizes flexible regulation of the gas product components and effectively improves the wide-range adaptability of biomass gasification products in application scenarios.

[0058] (3) Control optimization: Based on the gas component data information of the monitoring points, the CO2 conversion rate and the carbon recovery rate are calculated, the regulation flow rate of the gas input unit during the regulation process is calculated, and the control strategy instructions are formed and transmitted to the electronic flow controller of the gas input unit, so that the corresponding CO2 flow regulation is quickly made, realizing in-situ regeneration of the catalyst and carbon-rich gas regulation.

[0059] The above examples are only for illustrating the technical concept and characteristics of the present application, and the purpose is to enable those skilled in the art to understand the present application and to implement it, and cannot limit the protection scope of the present application. Any equivalent changes or modifications made according to the essence of the present application should be covered within the protection scope of the present application.

Claims

1. A biomass gasification device for producing carbon-rich fuel gas based on in-situ catalyst regeneration, characterized in that: It includes a biomass input unit, a gas input unit and a reaction unit; The biomass input unit is used to adjust the biomass feed amount to transport the biomass to the reaction unit; The gas input unit is used to adjust the flow rate of the gas and introduce it into the reaction unit; the gas includes air and CO2; The reaction unit includes, from top to bottom, a reforming zone, a gasification zone and a residue combustion zone; the biomass is transported to the gasification zone, and air is introduced into the gasification zone to react with the biomass to generate combustible gas. The solid residue generated after the biomass gasification falls into the residue combustion zone for combustion, and the heat generated by the combustion is transferred to the gasification zone and the reforming zone to provide heat for gasification and reforming; the reforming zone includes a fuel gas reforming zone and a CO2 reforming zone; the combustible gas generated in the gasification zone is introduced into the fuel gas reforming zone, and the CO2 is introduced into the CO2 reforming zone, and the combustible gas and CO2 react with the oxidized and reduced catalysts respectively to generate CO-rich fuel gas and discharge it from the reaction unit.

2. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 1 is characterized in that: It also includes a gas product collection unit, including a negative pressure gas storage tank, which is connected to the reaction unit and is used to collect CO-rich fuel gas, promote gas flow in the reaction unit, and promote desorption during the gas reaction process.

3. The biomass gasification device for producing carbon-rich fuel gas based on in-situ catalyst regeneration according to claim 1 or 2, characterized in that: The gas input unit includes an electronic flow controller to adjust the flow of air and CO2 using the electronic flow controller.

4. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 3 is characterized in that: It also includes a gas monitoring unit for real-time monitoring of the distribution of gas components in the reaction unit to calculate the CO2 conversion rate and carbon recovery rate, and to form control strategy instructions to be transmitted to the electronic flow controller of the gas input unit to regulate the CO2 flow.

5. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 4 is characterized in that: The gas monitoring unit includes gas monitoring point one, gas monitoring point two and gas monitoring point three; gas monitoring point one is set at the air inlet of the fuel gas reforming zone, gas monitoring point two is set at the air outlet of the CO2 reforming zone, and gas monitoring point three is set at the discharge port of the CO-rich fuel gas.

6. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 5 is characterized in that: The carbon recovery rate of the reforming process is calculated using the gas composition data of gas monitoring point one and gas monitoring point three; the CO2 conversion rate is calculated using the CO2 inlet flow rate and the gas composition data of gas monitoring point two.

7. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 6 is characterized in that: The reforming zone is composed of a honeycomb reactor, the catalyst active material of the honeycomb reactor is composed of a composite metal oxide of a transition metal and a lanthanide metal; the catalyst active material and a binder are mixed and molded into a honeycomb shape and placed in the honeycomb reactor.

8. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 7 is characterized in that: The ratio of the transition metal to the lanthanide metal is in the range of 1 to 1.

2.

9. The biomass gasification and carbon-rich fuel gas production device based on in-situ catalyst regeneration according to claim 7, characterized in that: The reforming zone also includes an upper transition zone and a lower transition zone; the honeycomb reactor is driven by a motor to rotate, so that the catalyst circulates through the gas reforming zone, the upper transition zone, the CO2 reforming zone and the lower transition zone.

10. A method for producing carbon-rich fuel gas by biomass gasification based on in-situ catalyst regeneration, based on the device according to claim 7, characterized in that: The method comprises the following steps: Air is introduced into the gasification zone, and the gasification zone is heated from room temperature to gasification temperature by an external heat source. Then, biomass is input through a conveyor belt, and air is introduced into the gasification zone to react with the biomass. The gasification residue produced by gasification enters the residue combustion zone, and the heat of combustion is transferred to the reforming zone to provide heat for the reforming of the gasification products; The gas product from the gasification zone is introduced into the fuel gas reforming area, where the gas reacts with the oxidized catalyst to consume H2 with strong reducing activity, while converting the catalyst into a reduced state. As the honeycomb reactor rotates, the reduced catalyst rotates to the CO2 reforming area for oxidative regeneration, while reducing CO2 to produce CO. The carbon recovery rate of the reforming process is calculated using the gas composition data from gas monitoring points one and three, and the CO2 conversion rate is calculated using the CO2 inlet flow rate and the gas composition data from gas monitoring point two. If the CO2 conversion rate < N%, control the reduction of the CO2 flow rate according to the CO2 conversion rate and the CO2 inlet flow rate; where the CO2 conversion rate calculation formula is X CO2 =(V in- V out ) / V in , where V in is the CO2 inlet flow rate, obtained by reading the electronic flow controller of the gas input unit, and V out is the CO2 inlet flow rate at gas monitoring point 2, obtained by reading the gas chromatography test results; the calculation formula for the reduction amount of CO2 during the process of regulating the CO2 flow rate is V down =(N% - X CO2 )×V in ; If the CO2 conversion rate ≥ N% and the carbon recovery rate < M%, increase the CO2 flow rate according to the carbon recovery rate and the gas flow rate at the inlet of the reforming zone; among them, the calculation formula of the carbon recovery rate where V in-co and are the inlet flow rates of CO and CO2 at gas monitoring point 2, is the flow rate of various short-chain hydrocarbon gases at gas monitoring point 2, obtained by reading the gas chromatography test results; V in-co 、 and are the flow rates of CO, CO2 and various short-chain hydrocarbon gases at gas monitoring point 3, respectively, obtained by reading the gas chromatography test results; the formula for the increase in CO2 during the process of regulating the CO2 flow rate is N and M are natural numbers.

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