Internal circulating fluidized bed reaction device

Abstract

The utility model relates to the technical field of gas-solid two-phase fluidization, in particular to an internal circulating fluidized bed reaction device. The device comprises a reaction unit, a gas supply unit and a heat transfer turbulent flow unit, a vertical center partition plate and a gas inlet partition plate are arranged in a reaction shell of the reaction unit, an inner cavity is divided into a high-speed cavity and a low-speed cavity, the two cavities are communicated above the center partition plate, and the top of each cavity extends towards the low-speed cavity to form a first side-inclined partition plate; the gas supply unit injects gas into the bottoms of the two cavities respectively, the heat transfer turbulent flow unit is arranged in the reaction shell, heat exchange and sine wave turbulent flow are carried out in the high-speed cavity, and the feeding pipe and the discharging pipe are arranged on the upper portion and the lower portion of the shell respectively. According to the utility model, the gas-solid two-phase contact efficiency, the heat transfer performance and the operation stability in the reactor are integrally improved, and an efficient and reliable reaction device solution is provided for the chemical looping hydrogen production process of low-grade fuel such as semi-coke tail gas.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of gas-solid fluidization, especially to an internal circulation fluidized bed reaction device. BACKGROUND

[0002] A large amount of semi-coke tail gas is produced in the semi-coke production process, with a huge annual output. The semi-coke tail gas is rich in hydrogen, carbon monoxide, methane and other high-value chemical raw materials. However, the semi-coke tail gas also contains tar, benzene, naphthalene, phenol, dust, sulfides, ammonia and heavy metals and other complex impurities, which poses a great challenge to the efficient and clean resource utilization of the semi-coke tail gas. At present, most semi-coke enterprises are limited by technical bottlenecks and can only directly burn the tail gas as low-value fuel, which not only causes serious waste of valuable chemical resources, but also causes environmental pollution. Therefore, developing a technology that can efficiently convert the reducing components in the semi-coke tail gas into high-value-added products (such as high-purity hydrogen) is of great significance for realizing resource recycling and clean energy development.

[0003] Chemical looping technology, especially chemical looping hydrogen production technology, provides a promising path to achieve this goal. The technology usually involves two core reaction zones: in the fuel reactor, carbon-containing fuels (such as CO, , in the semi-coke tail gas) have a reduction reaction with an oxygen carrier, and the oxygen carrier loses lattice oxygen and is reduced; in the steam reactor, the reduced oxygen carrier has an oxidation reaction with steam, regains lattice oxygen and releases hydrogen. The circulation of the oxygen carrier between the two reactors realizes the directional transfer of matter and energy. This process theoretically has the advantages of high efficiency, low energy consumption and easy separation of product gas. However, the industrial application of this technology is highly dependent on high-performance reactors that can achieve efficient mass transfer, heat transfer and stable solid circulation between the gas and solid phases.

[0004] Traditional fixed bed or conventional fluidized bed reactors have significant defects when applied to such chemical looping processes. Fixed bed reactors have poor heat transfer performance and are prone to hot spots, and the reaction-regeneration operation needs to be switched intermittently. Although the conventional fluidized bed improves heat transfer, the gas-solid flow structure is difficult to control accurately, and there is a common phenomenon of gas "short circuiting" or "bypassing", i.e. part of the reaction gas quickly passes through the bed without fully contacting the solid particles, resulting in a decrease in the conversion rate of the reactants. At the same time, "dead zones" with slow or stagnant flow are easily formed inside the bed, causing uneven distribution of solid particles, incomplete local reaction and heat accumulation. In addition, maintaining a sufficient and controllable solid particle circulation rate is crucial for the continuous operation of chemical looping technology, and the structure of traditional fluidized beds often makes it difficult to strengthen solid circulation without exacerbating gas bypassing, resulting in a mismatch between heat, mass and reaction processes, and making it difficult to further improve the overall thermal conversion efficiency and product gas (such as hydrogen) concentration.

[0005] To overcome the above problems, the internally circulating fluidized bed (ICFB) is proposed. By setting a vertical partition in a single reactor shell, the bed is physically separated into high-speed and low-speed zones, and the static pressure difference between the two zones is used to drive the internal circulation of solid particles. This structure theoretically has the potential to organize reduction and oxidation reactions (or enhance heat and mass transfer) in different zones within the same device. However, the existing conventional ICFB structure still has many problems. First, due to the low gas velocity, the low-speed zone has poor fluidization state of particles, and "dead zones" are easily formed at the bottom or corners, which leads to the ineffective participation of part of the oxygen carrier in circulation and reaction, reducing the overall utilization rate. Second, the gas bypass problem is still prominent, and part of the reaction gas may directly flow from the high-speed zone to the outlet through the upper communication area, or bypass the main reaction area through an unreasonable flow path, reducing the gas-solid contact efficiency. Third, there is a contradiction between solid circulation rate and gas distribution: in order to enhance the solid circulation, a certain pressure difference is needed, but this may exacerbate the unevenness of gas distribution and bypass; and the structural measures taken to suppress bypass may hinder the smooth circulation of solids. The existing structure often has difficulty in achieving a good balance between suppressing gas bypass, eliminating flow dead zones, and maintaining sufficient solid circulation rate, resulting in poor temperature distribution uniformity inside the reactor, limited heat transfer efficiency, and uneven chemical reaction rate, ultimately restricting the hydrogen production rate and the energy conversion efficiency of external heat sources such as solar energy. Therefore, it is necessary to optimize the internal structure of the traditional ICFB reactor to optimize the gas-solid flow, heat transfer and reaction process. Practical new type content

[0006] The technical problem to be solved by the embodiments of the present utility model lies in providing an internal circulating fluidized bed reactor to solve the problems of high gas bypass rate, difficult simultaneous control of flow dead zones in the low-speed zone and solid circulation rate in the traditional partition type internal circulating fluidized bed reactor in the prior art.

[0007] The utility model discloses an internal circulating fluidized bed reaction device, including reaction unit, gas supply unit and heat transfer turbulence unit,

[0008] The reaction unit includes a reaction shell, and a partition assembly arranged in the reaction shell, the partition assembly includes a vertically arranged center partition and a gas inlet partition, and the center partition separates the internal space of the reaction shell into a high-speed chamber and a low-speed chamber.

[0009] The gas supply unit includes a first gas injection assembly and a second gas injection assembly, the first gas injection assembly is connected with the reaction shell, and forms a high-speed gas injection inlet at the bottom of the high-speed chamber, and the second gas injection assembly is connected with the reaction shell, and forms a low-speed gas injection inlet at the bottom of the low-speed chamber.

[0010] The upper part of the reaction shell is provided with a feeding pipe for injecting solid-phase particles into the low-speed chamber, and the lower part of the reaction shell is provided with a discharging pipe for discharging solid-phase particles from the low-speed chamber;

[0011] The high-speed chamber and the low-speed chamber are in communication above the central partition plate, and the top of the central partition plate extends obliquely upwards to form a first oblique partition plate above the low-speed chamber; the high-speed chamber and the low-speed chamber are in communication below the central partition plate, the air inlet partition plate is fixedly arranged on the inner bottom surface of the low-speed chamber to separate the central partition plate and the low-speed air inlet, and a circulation gap for guiding the flow of solid-phase particles from the low-speed chamber to the high-speed chamber is formed between the central partition plate and the air inlet partition plate;

[0012] The heat transfer disturbance unit is arranged on the reaction shell and performs heat exchange and sinusoidal wave disturbance on the airflow flowing through the high-speed chamber.

[0013] Optionally, the bottom of the central partition plate is higher than the top of the air inlet partition plate, the bottom of the central partition plate extends obliquely downwards to form a second oblique partition plate below the low-speed chamber, and the bottom of the second oblique partition plate extends downwards to form a flow guide partition plate parallel to the central partition plate.

[0014] The high-speed chamber and the low-speed chamber are in communication below the flow guide partition plate, and the circulation gap is formed between the flow guide partition plate and the air inlet partition plate.

[0015] Optionally, the top of the air inlet partition plate is flush with the top of the flow guide partition plate, and the air inlet partition plate is an inclined structure with the top obliquely away from the flow guide partition plate.

[0016] Optionally, the first air injection assembly comprises a first air injection pipe and a first air cap, one end of the first air injection pipe is connected to a high-speed gas source, the other end of the first air injection pipe is connected to the bottom of the high-speed chamber and is vertically fixed in the high-speed chamber, and the first air cap is fixedly arranged on the port of the first air injection pipe in the high-speed chamber to regulate the high-speed gas injected into the high-speed chamber.

[0017] Optionally, the second air injection assembly comprises a second air injection pipe and a second air cap, one end of the second air injection pipe is connected to a low-speed gas source, the other end of the second air injection pipe is connected to the bottom of the low-speed chamber and is vertically fixed in the low-speed chamber, and the second air cap is fixedly arranged on the port of the second air injection pipe in the low-speed chamber to regulate the low-speed gas injected into the low-speed chamber.

[0018] Optionally, a plurality of air outlet holes are formed in the circumferential direction on the first hood and the second hood.

[0019] Optionally, the bottom of the flow guide partition is higher than the first hood, and the top of the gas inlet partition is higher than the second hood.

[0020] Optionally, the heat transfer disturbance unit comprises a heat conduction plate and a disturbance plate, the heat conduction plate is fixed on the outer sidewall of the reaction shell to perform heat transfer on the high-speed chamber, and the disturbance plate is distributed in the high-speed chamber in the width direction of the center partition.

[0021] One sidewall of the disturbance plate is fixed on the inner sidewall of the reaction shell, and a flow channel for upward movement of gas flow is formed between two adjacent disturbance plates, the other sidewall of the disturbance plate is in a continuous sinusoidal wave shape in the vertical direction, and the flow channel forms periodic contraction sections and expansion sections in the vertical direction.

[0022] Optionally, the heat transfer disturbance unit comprises a plurality of electric heating pipes distributed in the high-speed chamber in the width direction of the center partition, the electric heating pipes are vertically arranged, and the electric heating pipes are in a continuous sinusoidal wave shape in the vertical direction, the top end and the bottom end of the electric heating pipes extend outside the reaction shell for external power connection.

[0023] Optionally, the feeding pipe is located above the first inclined partition, and the feeding pipe is in an inclined structure with a feeding direction inclined towards the low-speed chamber, the discharging pipe is located above the gas inlet partition, and the discharging pipe is in an inclined structure with a discharging direction inclined downwards, and the reaction shell is further provided with a gas outlet at the top.

[0024] Compared with the prior art, the internal circulating fluidized bed reaction device provided in the embodiment of the utility model has the beneficial effects that:

[0025] Through the cooperation of the center partition and the gas inlet partition in the reaction unit and the action of the heat transfer disturbance unit, the gas-solid flow between the high-speed chamber and the low-speed chamber can be effectively and cooperatively controlled. The center partition and the first inclined partition at the top thereof optimize the gas flow guiding and particle distribution in the upper communication region and inhibit the gas bypassing. The circulation gap formed by the gas inlet partition and the bottom of the center partition ensures the orderly backflow of the solid particles from the low-speed chamber to the high-speed chamber while isolating the low-speed gas injection inlet, and eliminates the flow dead zone at the bottom of the low-speed chamber. Meanwhile, the heat transfer disturbance unit simultaneously realizes the strengthened heat transfer and the sinusoidal wave disturbance in the high-speed chamber, further uniformizes the bed temperature and improves the fluidization quality. Thus, based on the cooperative action of the structures of the units, the gas-solid contact efficiency, the heat transfer performance and the flow stability in the reactor are comprehensively improved without sacrificing the solid circulation. BRIEF DESCRIPTION OF DRAWINGS

[0026] The technical solutions of the utility model will be further explained in detail in combination with the drawings and embodiments, wherein:

[0027] Figure 1 The whole structure schematic diagram of the internal circulation fluidized bed reaction device provided by the utility model embodiment is shown in the figure;

[0028] Figure 2 The structure schematic diagram of the electric heating tube assembly provided by the utility model embodiment is shown in the figure;

[0029] Figure 3 The waveform structure schematic diagram of the electric heating tube provided by the utility model embodiment is shown in the figure;

[0030] Figure 4 The temperature distribution diagram of each measuring point when the gas speed ratio in the high-speed chamber and the low-speed chamber is 1 / 1

[0031] Figure 5 The temperature distribution diagram of each measuring point when the gas speed ratio in the high-speed chamber and the low-speed chamber is 2 / 1

[0032] The marks in the drawings represent as follows:

[0033] 1, reaction shell; 11, high-speed chamber; 12, low-speed chamber; 2, center partition; 21, first side-inclined partition; 22, second side-inclined partition; 23, flow guide partition; 3, gas inlet partition; 4, first gas injection assembly; 41, first gas injection pipe; 42, first air cap; 5, second gas injection assembly; 51, second gas injection pipe; 52, second air cap; 6, feeding pipe; 7, discharging pipe; 8, heat transfer and flow disturbance unit; 81, heat conduction plate; 82, flow disturbance plate; 83, electric heating tube; 9, gas outlet. DETAILED DESCRIPTION

[0034] It should be noted that the embodiments in the present application and the features in the embodiments can be combined with each other without conflict. The preferred embodiments of the utility model will be explained in detail in combination with the drawings.

[0035] The utility model discloses an internal circulation fluidized bed reaction device, as shown in the figure, including reaction unit, gas supply unit and heat transfer and flow disturbance unit 8. Figure 1

[0036] The reaction unit includes a reaction shell 1 and a partition assembly arranged in the reaction shell 1, and the partition assembly includes a center partition 2 arranged vertically and a gas inlet partition 3, and the center partition 2 divides the internal space of the reaction shell 1 into a high-speed chamber 11 and a low-speed chamber 12. ​​​

[0037] The gas supply unit comprises a first gas injection assembly 4 and a second gas injection assembly 5, the first gas injection assembly 4 is connected with the reaction shell 1 and forms a high-speed gas injection inlet at the bottom of the high-speed chamber 11, and the second gas injection assembly 5 is connected with the reaction shell 1 and forms a low-speed gas injection inlet at the bottom of the low-speed chamber 12;

[0038] The upper part of the reaction shell 1 is provided with a feeding pipe 6 for injecting solid-phase particles into the low-speed chamber 12, and the lower part of the reaction shell 1 is provided with a discharging pipe 7 for discharging the solid-phase particles from the low-speed chamber 12;

[0039] The high-speed chamber 11 and the low-speed chamber 12 are connected above the center partition plate 2, and the top of the center partition plate 2 extends upward to form a first side tilt partition plate 21 above the low-speed chamber 12, and the high-speed chamber 11 and the low-speed chamber 12 are connected below the center partition plate 2, and the gas inlet partition plate 3 is fixedly arranged on the inner bottom surface of the low-speed chamber 12 to separate the center partition plate 2 and the low-speed gas injection inlet, and a circulation gap for guiding the solid-phase particles to flow from the low-speed chamber 12 to the high-speed chamber 11 is formed between the center partition plate 2 and the gas inlet partition plate 3;

[0040] The heat transfer disturbance unit 8 is arranged on the reaction shell 1 and performs heat exchange and sinusoidal wave disturbance on the gas flow passing through the high-speed chamber 11.

[0041] Through the implementation of the above-mentioned internal circulating fluidized bed reaction device embodiment, the reaction shell 1 in the reaction unit provides a core closed reaction space, and the center partition plate 2 divides the entire internal space into the high-speed chamber 11 and the low-speed chamber 12 which exist in parallel and are connected with each other, thereby creating basic conditions for establishing a differentiated gas velocity field and particle circulation. The gas inlet partition plate 3 is a key internal component, which is fixedly arranged on the inner bottom surface of the low-speed chamber 12, and its primary function is to physically separate the low-speed gas inlet flow from the second gas injection assembly 5 and the connecting area at the bottom of the center partition plate 2, so as to force the solid-phase particles settled above the low-speed chamber 12 and possibly accumulated near the low-speed gas injection inlet to be lifted and guided to the other side of the gas inlet partition plate 3, thereby significantly reducing the risk of deposition of particles near the low-speed gas injection inlet to form a dead zone. At the same time, the circulation gap reserved between the gas inlet partition plate 3 and the bottom of the center partition plate 2 constitutes the only channel for the solid-phase particles to return from the low-speed chamber 12 to the high-speed chamber 11, thereby ensuring that while achieving gas path separation and optimization, the ordered backflow of the solid-phase particles along the preset path from the low-speed zone to the high-speed zone is guided and strengthened.

[0042] The first tilt partition 21 is formed by the top of the central partition 2 extending upwardly and deviating from the low-speed chamber 12, and the minimum angle between the first tilt partition 21 and the horizontal plane is preferably in the range of 10°-45°. The first tilt partition 21 changes the geometry and flow direction of the communication between the top of the high-speed chamber 11 and the low-speed chamber 12, and produces flow guiding and redistribution effects on the high-speed gas-solid mixture rising to the top, promotes the particle separation effect, and makes the particles more smoothly turn and enter the low-speed chamber 12. On the one hand, the first tilt partition 21 reduces the turbulence and back mixing of the gas in the top communication area, and reduces the bypass tendency of the gas directly flowing from the high-speed chamber 11 to the gas outlet 9 through a short circuit; on the other hand, the first tilt partition 21 also promotes the settling and separation of the particles at the top, and provides favorable conditions for the particles to enter the low-speed chamber 12 and complete the circulation.

[0043] The gas supply unit allows the gas flow rate, composition and pressure of the two chambers to be regulated separately by injecting gas into the bottom of the high-speed chamber 11 and the low-speed chamber 12 through the high-speed gas injection inlet and the low-speed gas injection inlet respectively, so that the required operating gas velocity ratio and pressure difference between the high-speed chamber 11 and the low-speed chamber 12 can be accurately established and maintained. The pressure difference is the fundamental driving force for the solid-phase particles to pass through the circulation gap to realize stable and controllable internal circulation, so that the solid circulation rate can be actively regulated to meet the needs of different reaction stages.

[0044] The feeding pipe 6 is arranged at the upper part of the reaction shell 1 and is used for injecting solid-phase particles into the low-speed chamber 12, and the discharging pipe 7 is arranged at the lower part and is used for discharging the particles in the low-speed chamber 12, thereby forming an external supplement and update path of the solid material, which is complementary to the internal circulation, and together maintains the stability of the total amount and activity of the particles in the bed.

[0045] The heat transfer disturbance unit 8 is integrated on the reaction shell 1 and acts on the high-speed chamber 11, and simultaneously performs efficient heat exchange and specific flow disturbance on the gas-solid two-phase flow passing through the high-speed chamber 11. The heat exchange function strengthens the heat input or removal process in the high-speed chamber 11, so that the reaction temperature can be accurately controlled and more uniformly distributed. The sinusoidal wave disturbance produces continuous cutting, turning and remixing effects on the main gas flow in the high-speed chamber 11 through its unique periodic wave surface structure, effectively breaks the stable gas flow channel or large bubbles that may be formed, and forces the gas and solid-phase particles to be more fully mixed and contacted in the radial direction, thereby significantly inhibiting the local short circuit or bypass phenomenon of the gas in the high-speed chamber 11. At the same time, the disturbance also enhances the movement of the particles near the wall, reduces the flow dead zone near the wall, and improves the fluidization quality of the overall bed.

[0046] Therefore, the internal circulation fluidized bed reaction device improves the gas-solid two-phase contact efficiency, heat transfer performance and operation stability in the reactor as a whole, and provides an efficient and reliable reaction device solution for the chemical chain hydrogen production process of low-grade fuels such as semicoke tail gas.

[0047] Further, the bottom of the center partition 2 is higher than the top of the air inlet partition 3, the bottom of the center partition 2 extends downward to form a second side tilt partition 22 below the low-speed chamber 12, and the bottom of the second side tilt partition 22 extends downward to form a flow guide partition 23 parallel to the center partition 2;

[0048] The high-speed chamber 11 and the low-speed chamber 12 are connected below the flow guide partition 23, and the flow guide partition 23 and the air inlet partition 3 form a circulation gap.

[0049] Through the implementation of the above-mentioned internal circulating fluidized bed reaction device embodiment, the bottom of the center partition 2 is higher than the top of the air inlet partition 3, which substantially raises the connection area of the bottom of the center partition 2, so that the solid phase particles entering the high-speed chamber 11 from the circulation gap can have more residence time in the connection area, which is beneficial to strengthen the gas-solid reaction. The air inlet partition 3 separates the space directly connecting the bottom of the low-speed chamber 12 and the bottom of the high-speed chamber 11, forcing the solid phase particles settled above the low-speed chamber 12 and the particles that may accumulate near the low-speed air injection inlet to be forced to rise and be guided to the other side of the air inlet partition 3, thereby significantly reducing the risk of particles depositing near the low-speed air injection inlet to form a dead zone.

[0050] In addition, the second side tilt partition 22 formed by the bottom of the center partition 2 extending downward below the low-speed chamber 12 serves as an inclined flow guide surface, smoothly guiding the particles collected there to the circulation gap defined by the flow guide partition 23 and the air inlet partition 3. The high-speed chamber 11 and the low-speed chamber 12 are connected below the flow guide partition 23, and the circulation gap formed between the flow guide partition 23 and the air inlet partition 3 is significantly shortened. The shortened gap has an accelerating effect on the airflow passing through the gap, which can more effectively drag and guide the solid phase particles into the high-speed chamber 11, further avoiding the deposition and residence of particles near the air inlet partition 3, and ensuring the smooth and efficient backflow of the bottom particles to the high-speed chamber 11.

[0051] Therefore, the embodiment of the utility model utilizes the high-position structure of the bottom of the center partition 2, the separation and flow guiding effect of the air inlet partition 3, and the guiding and accelerating channel formed by the second side tilt partition 22 and the flow guide partition 23, effectively prevents the formation of a dead zone at the bottom of the low-speed chamber 12, ensures and optimizes the internal circulation path and efficiency of the solid particles, and improves the reaction efficiency by increasing the residence time of the particles in the high-speed chamber 11, thereby overall strengthening the solution effect of the coordinated control problem of gas bypass, flow dead zone and solid circulation rate.

[0052] Further, the top of the air inlet partition 3 is flush with the top of the flow guide partition 23, and the air inlet partition 3 is an inclined structure with the top deviating away from the flow guide partition 23.

[0053] By implementing the above-mentioned embodiment of the internal circulating fluidized bed reaction device, the top of the gas inlet partition plate 3 is flush with the top of the guide partition plate 23, so that the circulating gap inlet plane jointly defined by the two is lifted as a whole. As a result, the solid-phase particles that have settled down from above the low-speed chamber 12 have a relatively higher inlet position when entering the circulating gap, thereby further prolonging the residence time of the solid-phase particles in the high-speed chamber 11, so as to strengthen the gas-solid mass transfer and reaction process.

[0054] The gas inlet partition plate 3 adopts an inclined structure with the top deviated away from the guide partition plate 23, and the minimum included angle between the gas inlet partition plate 3 and the horizontal plane is preferably in the range of 5°-30°. On the one hand, a tapered gas flow channel with a gradually decreasing cross-sectional area is formed above the low-speed gas injection inlet. The tapered structure accelerates the low-speed gas flow from the second gas injection assembly 5, so as to enhance the lifting capacity of the solid-phase particles above the low-speed gas injection inlet, and help to prevent the solid-phase particles that have settled down above from accumulating to form a dead zone near the low-speed gas injection inlet. At the same time, the circulating gap formed between the inclined gas inlet partition plate 3 and the guide partition plate 23 presents a gradually expanding geometric feature along the gas flow direction (from the low-speed chamber 12 side to the high-speed chamber 11 side). This gradually expanding structure provides a smoother flow path for the solid-phase particles above the gas inlet partition plate 3 in the low-speed chamber 12, and can guide more particles to enter the high-speed chamber 11 through the circulating gap more quickly and more concentratedly, thereby effectively promoting the internal circulation flux of the solid material between the high-speed and low-speed chambers 11 and 12.

[0055] Therefore, the embodiments of the present application not only improve the reaction efficiency by prolonging the residence time of the particles in the high-speed chamber 11, but also improve the fluidization state at the bottom of the low-speed chamber 12 by the inclined gas inlet partition plate 3. These structures synergistically strengthen the inhibition of gas bypassing, the elimination of the flow dead zone at the bottom of the low-speed chamber 12, and the stable maintenance of the solid circulation rate.

[0056] Further, the first gas injection assembly 4 includes a first gas injection pipe 41 and a first air cap 42. One end of the first gas injection pipe 41 is connected to a high-speed gas source, and the other end of the first gas injection pipe 41 is connected to the bottom of the high-speed chamber 11 and is vertically fixed in the high-speed chamber 11. The first air cap 42 is fixed to the port of the first gas injection pipe 41 in the high-speed chamber 11, and is used to straighten the high-speed gas injected into the high-speed chamber 11.

[0057] Further, the second gas injection assembly 5 includes a second gas injection pipe 51 and a second air cap 52. One end of the second gas injection pipe 51 is connected to a low-speed gas source, and the other end of the second gas injection pipe 51 is connected to the bottom of the low-speed chamber 12 and is vertically fixed in the low-speed chamber 12. The second air cap 52 is fixed to the port of the second gas injection pipe 51 in the low-speed chamber 12, and is used to straighten the low-speed gas injected into the low-speed chamber 12.

[0058] Further, a plurality of gas outlet holes are formed circumferentially on the first air cap 42 and the second air cap 52.

[0059] Through the implementation of the above-mentioned internal circulating fluidized bed reaction device embodiment, one end of the first gas injection pipe 41 is connected to a high-speed gas source, and the other end is connected to the bottom of the high-speed chamber 11 and is vertically fixed therein, so that the high-speed gas can be injected from the bottom of the high-speed chamber 11 and form a vertically upward high-speed gas flow; similarly, one end of the second gas injection pipe 51 is connected to a low-speed gas source, and the other end is connected to the bottom of the low-speed chamber 12 and is vertically fixed therein, so that the low-speed gas can be directly injected from the bottom of the low-speed chamber 12 and form a vertically upward low-speed gas flow. Thus, the gas can enter from the bottom closest to the solid particle accumulation area, which is conducive to quickly starting and maintaining the fluidization at the bottom of each chamber.

[0060] The first air cap 42 fixed at the port of the first gas injection pipe 41 regulates the injected high-speed gas, and the second air cap 52 fixed at the port of the second gas injection pipe 51 regulates the injected low-speed gas. The core function of the two air caps is to disperse and redistribute the concentrated flow from the respective gas injection pipes. The plurality of gas outlet holes formed circumferentially on the first air cap 42 and the second air cap 52 are the key to effective regulation. These circumferentially distributed gas outlet holes disperse the gas into multiple fine streams with different directions, thereby forming a relatively uniform and diffuse gas flow distribution area around the air cap. Thus, the local channeling, gas bypassing, or excessive flushing damage to the bottom particle structure caused by the concentrated jet of high-speed gas or low-speed gas is avoided.

[0061] The high-speed gas regulated by the first air cap 42 forms a uniform upward gas flow at the bottom of the high-speed chamber 11, providing stable lifting force for the particles; the low-speed gas regulated by the second air cap 52 forms a stable fluidizing gas flow at the bottom of the low-speed chamber 12, which helps to prevent the accumulation of particles near the gas inlet to form a dead zone, and maintains the necessary fluidization state in this area to support the movement of particles to the circulating gap. Therefore, this structure of bottom gas inlet combined with circumferential multi-hole regulation of the air cap effectively reduces the bypassing tendency and improves the fluidization quality at the bottom of the two chambers, thereby creating favorable initial conditions for establishing the expected pressure difference between the high-speed chamber 11 and the low-speed chamber 12 and driving the solid particles to pass through the circulating gap to achieve stable and orderly internal circulation.

[0062] Further, the bottom of the flow guide partition 23 is higher than the first air cap 42, and the top of the gas inlet partition 3 is higher than the second air cap 52.

[0063] By implementing the above-mentioned internal circulating fluidized bed reaction device embodiment, the bottom of the flow guide partition 23 is higher than the first air cap 42, which essentially raises the communication area at the bottom of the flow guide partition 23. On the one hand, it helps the solid-phase particles entering the high-speed chamber 11 from the low-speed chamber 12 side via the circulating gap to be directly lifted by the high-speed gas injected; on the other hand, it provides a larger flow space, which can prolong the residence time of the solid-phase particles in the high-speed chamber 11, creating more sufficient conditions for the mass transfer and reaction process between the gas and solid phases. In addition, the top of the gas inlet partition 3 is higher than the second air cap 52, which essentially raises the circulating gap defined by the gas inlet partition 3 and the flow guide partition 23, thereby prolonging the residence time of the solid-phase particles entering the high-speed chamber 11 to strengthen the gas-solid mass transfer and reaction process. Further, the smooth and stable circulation of the solid-phase particles between the high-speed and low-speed chambers 12 via the circulating gap is ensured by the cooperation of the two, thereby deepening the inhibition of gas bypassing tendency, eliminating flow dead zones, and maintaining solid circulation rate.

[0064] Preferably, assuming the width of the reaction shell 1 is D, the distance from the bottom of the flow guide partition 23 to the bottom surface of the reaction shell 1 is in the range of 0.1D-0.3D, the distance between the flow guide partition 23 and the gas inlet partition 3 is in the range of 0.05-0.25D, and the particle size of the solid-phase particles is in the range of 200-500 , and BF3 , represents an oxygen carrier filler composed of barium (Ba), iron (Fe), aluminum (Al), and oxygen (O) elements.

[0065] Further, the heat transfer disturbance unit 8 includes a heat conduction plate 81 and a disturbance plate 82, the heat conduction plate 81 is fixedly arranged on the outer side wall of the reaction shell 1 to conduct heat to the high-speed chamber 11, and the disturbance plate 82 is distributed in parallel along the width direction of the center partition 2 in the high-speed chamber 11;

[0066] One side wall of the disturbance plate 82 is fixedly arranged on the inner side wall of the reaction shell 1, and a flow channel for the gas to move upward is formed between adjacent two disturbance plates 82. The other side wall of the disturbance plate 82 is in a continuous sinusoidal wave shape in the vertical direction, and the flow channel forms periodic contraction sections and expansion sections in the vertical direction.

[0067] By implementing the above-mentioned internal circulating fluidized bed reaction device embodiment, the heat conduction plate 81 is used as an efficient heat transfer interface between the external heat source (such as solar heating) and the reaction area in the high-speed chamber 11, which can stably and uniformly introduce heat into the high-speed chamber 11, which is conducive to maintaining and adjusting the temperature environment required for the reaction in the high-speed chamber 11.

[0068] Secondly, the high-speed chamber 11 is divided into multiple parallel sub-channels by the multiple spoiler plates 82, the ascending airflow is physically divided, and the flow channel formed between the adjacent two spoiler plates 82 provides a clear ascending path for the gas-solid two-phase flow, thereby laying a foundation for implementing fine flow regulation. One side wall of the spoiler plate 82 is in a continuous sinusoidal wave shape in the vertical direction, so that the flow channel forms periodic contraction sections and expansion sections in the vertical direction. The periodically changing channel geometry forces the flowing gas and the carried particles to undergo repeated acceleration and deceleration movements: the gas flow is accelerated in the contraction section, the shear effect is enhanced, and the gas-solid mixing is promoted; in the expansion section, the gas flow is decelerated, the pressure is recovered, and controllable vortexes are generated, further strengthening the transverse mixing. This dynamic and orderly disturbance effectively breaks the possible laminar flow or plug flow, greatly suppresses the tendency of gas "short circuiting" or bypassing in the flow channel, eliminates the flow dead zone near the wall, and significantly improves the uniformity and stability of the bed layer fluidization.

[0069] Therefore, the embodiment of the utility model combines the enhanced heat transfer provided by the heat conduction plate 81 and the disturbance induced by the sinusoidal wave shape of the spoiler plate 82, optimizes the temperature field and velocity field distribution in the high-speed chamber 11, makes the heat transfer and mass transfer more matched, and improves the reaction efficiency. Therefore, it is helpful to effectively deal with the gas bypassing and dead zone problem, and indirectly supports stable solid circulation by improving the fluidization quality, especially applicable to the implementation of solar energy supply scene.

[0070] Further, as shown in Figure 2 and Figure 3 The heat transfer and disturbance unit 8 includes multiple electric heating pipes 83 arranged side by side along the width direction of the center partition plate 2 in the high-speed chamber 11, the electric heating pipes 83 are vertically arranged, and the electric heating pipes 83 are in a continuous sinusoidal wave shape in the vertical direction, the top end and the bottom end of the electric heating pipes 83 respectively extend out of the reaction shell 1 for external power supply.

[0071] Through the implementation of the above-mentioned internal circulating fluidized bed reaction device embodiment, the multiple electric heating pipes 83 arranged side by side along the width direction of the center partition plate 2 in the high-speed chamber 11 divide the high-speed chamber 11 space into multiple parallel sub-regions, physically divide the ascending airflow, and create conditions for implementing the flow and heating management of the sub-regions and the whole. The electric heating pipes 83 are vertically arranged, so that the axial direction is consistent with the direction of the main flow, thereby maximizing the contact length and area with the gas-solid two-phase flow.

[0072] The electric heating tube 83 is in a continuous sinusoidal wave shape in the vertical direction. On the one hand, as a resistance heating element, when it is powered on, the sinusoidal wave-shaped tube body can directly and efficiently convert electrical energy into heat energy, and through its increased surface area, it can radiate and convect heat to the surrounding flowing gas and solid particles, achieving direct and uniform injection of heat inside the high-speed chamber 11, and strengthening the volume heat transfer process inside the bed.

[0073] The top and bottom ends of the electric heating tube 83 extend outside the reaction shell 1 for external power supply, which can ensure the controllability of heating power input, the safety of electrical connection and the convenience of maintenance, and at the same time avoids the difficulty of arranging complex electrical interface inside the high-temperature reactor. Therefore, this structure integrates the heating function and the sinusoidal wave flow disturbance structure, which simultaneously realizes efficient and uniform direct electric heating and active flow disturbance in the high-speed chamber 11, optimizes the reaction temperature field and flow field, thereby strengthening heat transfer, suppressing bypass and dead zones, improving fluidization quality, and indirectly supporting stable solid internal circulation, especially suitable for the implementation of green electricity power supply scene.

[0074] Further, the feed pipe 6 is located above the first side inclined baffle 21, and the feed pipe 6 is an inclined structure with the feed direction inclined towards the low-speed chamber 12, and the discharge pipe 7 is located above the air inlet baffle 3, and the discharge pipe 7 is an inclined structure with the discharge direction inclined downward, and the top of the reaction shell 1 is also provided with a gas outlet 9.

[0075] Through the implementation of the above-mentioned internal circulating fluidized bed reaction device embodiment, by using the feed pipe 6 located above the first side inclined baffle 21, and the feed direction inclined towards the low-speed chamber 12, the added solid particles can be injected from the area close to the top of the low-speed chamber 12, and can be guided by gravity to fall into the low-speed chamber 12 along the preset direction, ensuring that the particles accurately enter the predetermined area.

[0076] At the same time, by using the discharge pipe 7 located above the air inlet baffle 3, and the discharge direction inclined downward, it is convenient to extract the particles after reaction or need to be replaced, and the gravity and possible auxiliary power are used to promote the smooth discharge of the particles.

[0077] In addition, the gas outlet 9 provided at the top of the reaction shell 1 provides a concentrated escape channel for the gaseous products after gas-solid separation, and the top position conforms to the natural upward trend of the hot gas flow, which is beneficial to the preliminary separation of gas and heavier solid particles, so that the product gas can leave the reaction zone in time to maintain the reaction driving force.

[0078] In summary, the internal circulation fluidized bed reaction device of the embodiments of the present application can take into account the operation efficiency and the minimum interference to the internal core flow structure, so as to maintain the established gas-solid flow pattern and circulation stability in the reactor while ensuring continuous and stable operation, and indirectly support the coordinated control of the core problems such as gas bypass, dead zone and solid circulation.

[0079] As described above, the internal circulation fluidized bed reaction device of the present application directly affects the reaction characteristics, fluidization performance and wear behavior of the particles when applied in specific applications. Here, the temperature distribution, heating rate and spatial deviation of the internal circulation fluidized bed reaction device of the present application during the heating process from 25°C to 900°C are analyzed in detail:

[0080] A plurality of measuring points HT (HT-1 to HT-7 are evenly distributed in the high-speed chamber 11 and the low-speed chamber 12) are arranged in the reaction shell 1. As the heating process proceeds, the temperature of different measuring points (HT-1 to HT-7) in the reaction shell 1 gradually increases with time, but there is a certain difference in the temperature rising rate of each measuring point. In the initial heating stage, the heating rate of each measuring point is basically consistent, and the temperature distribution is uniform; however, when the temperature approaches the turning point of the fluidization state, there is a significant difference between the measuring points, especially the temperature rising rate of the middle measuring points such as HT-3, HT-4 and HT-5 is the fastest, showing a large temperature gradient. After reaching 600°C, the temperature of each measuring point tends to be stable, and the temperature distribution tends to be consistent, indicating that the bed has entered a stable fluidization state.

[0081] Further analysis is made from the experimental data of different high and low gas velocity ratios (H / L) / , wherein, H is the high apparent gas velocity, and H represents high gas velocity, L is the low apparent gas velocity, and L represents low gas velocity.

[0082] With the increase of the high and low gas velocity ratio, the left and right deviation of the temperature distribution in the reaction shell 1 is more obvious, especially the temperature difference between the high-speed chamber 11 and the low-speed chamber 12 is enlarged. As shown in Figure 4 , under the condition of / = 1 / 1 , the temperature distribution is relatively uniform, and the temperature of the high-speed chamber 11 is about 15°C higher than that of the low-speed chamber 12. This is because the raised center partition 2, the gas inlet partition 3 and the inclined first side inclined partition 21 strengthen the bed-wall heat transfer in the reaction shell 1. As shown in Figure 5 , when the gas velocity ratio increases to / =2 / 1 When the temperature distribution appears obvious fluctuation, the local area temperature exists larger deviation, which is related to the heat transfer inhomogeneous caused by the active particle movement and the frequent particle collision under the higher gas speed.

[0083] It should be understood that the above embodiments are only used to illustrate the technical solutions of the present application, but not to limit them. For those skilled in the art, the technical solutions recorded in the above embodiments can be modified, or some technical features can be replaced equivalently. All these modifications and replacements shall belong to the protection scope of the present application.

Claims

1. An internal circulating fluid bed reaction apparatus characterized by comprising: The internal circulating fluidized bed reaction device comprises a reaction unit, a gas supply unit and a heat transfer turbulence unit (8); The reaction unit comprises a reaction shell (1) and a partition assembly arranged in the reaction shell (1), wherein the partition assembly comprises a vertically arranged center partition plate (2) and a gas inlet partition plate (3), and the center partition plate (2) divides the internal space of the reaction shell (1) into a high-speed cavity (11) and a low-speed cavity (12); The gas supply unit comprises a first gas injection assembly (4) and a second gas injection assembly (5), wherein the first gas injection assembly (4) is connected with the reaction shell (1) and forms a high-speed gas injection inlet at the bottom of the high-speed cavity (11), and the second gas injection assembly (5) is connected with the reaction shell (1) and forms a low-speed gas injection inlet at the bottom of the low-speed cavity (12); The upper part of the reaction shell (1) is provided with a feeding pipe (6) for injecting solid-phase particles into the low-speed cavity (12), and the lower part of the reaction shell (1) is provided with a discharging pipe (7) for discharging the solid-phase particles from the low-speed cavity (12); The high-speed cavity (11) and the low-speed cavity (12) are connected above the center partition plate (2), and the top of the center partition plate (2) extends to the upper part of the low-speed cavity (12) to form a first side-inclined partition plate (21); the high-speed cavity (11) and the low-speed cavity (12) are connected below the center partition plate (2), and the gas inlet partition plate (3) is fixedly arranged on the inner bottom surface of the low-speed cavity (12) to divide the center partition plate (2) and the low-speed gas injection inlet, and a circulation gap for guiding the flow of solid-phase particles from the low-speed cavity (12) to the high-speed cavity (11) is formed between the center partition plate (2) and the gas inlet partition plate (3); The heat transfer turbulence unit (8) is arranged on the reaction shell (1) and performs heat exchange and sinusoidal wave turbulence on the gas flow passing through the high-speed cavity (11).

2. The internal circulation fluidized bed reaction apparatus according to claim 1, characterized by: The bottom of the center partition plate (2) is higher than the top of the gas inlet partition plate (3), the bottom of the center partition plate (2) extends to the lower part of the low-speed cavity (12) to form a second side-inclined partition plate (22), and the bottom of the second side-inclined partition plate (22) extends downward to form a flow guide partition plate (23) parallel to the center partition plate (2); The high-speed cavity (11) and the low-speed cavity (12) are connected below the flow guide partition plate (23), and the circulation gap is formed between the flow guide partition plate (23) and the gas inlet partition plate (3).

3. The internal circulation fluidized bed reaction apparatus according to claim 2, characterized by: The top of the gas inlet partition plate (3) is flush with the top of the flow guide partition plate (23), and the gas inlet partition plate (3) is an inclined structure with the top deviating away from the flow guide partition plate (23).

4. The internal circulation fluidized bed reaction apparatus according to claim 2, characterized by: The first gas injection assembly (4) comprises a first gas injection pipe (41) and a first air cap (42), one end of the first gas injection pipe (41) is connected with a high-speed gas source, the other end of the first gas injection pipe (41) is connected to the bottom of the high-speed chamber (11) and is vertically fixed in the high-speed chamber (11), and the first air cap (42) is fixed on the port of the first gas injection pipe (41) in the high-speed chamber (11) for rectifying the high-speed gas injected into the high-speed chamber (11).

5. The internal circulation fluidized bed reaction apparatus according to claim 4, characterized by: The second gas injection assembly (5) comprises a second gas injection pipe (51) and a second air cap (52), one end of the second gas injection pipe (51) is connected with a low-speed gas source, the other end of the second gas injection pipe (51) is connected to the bottom of the low-speed chamber (12) and is vertically fixed in the low-speed chamber (12), and the second air cap (52) is fixed on the port of the second gas injection pipe (51) in the low-speed chamber (12) for rectifying the low-speed gas injected into the low-speed chamber (12).

6. The internal circulation fluidized bed reaction apparatus according to claim 5, characterized by: A plurality of gas outlet holes are formed in the circumferential direction of the first air cap (42) and the second air cap (52).

7. The internal circulation fluidized bed reaction apparatus according to claim 5, characterized by: The bottom of the flow guide partition plate (23) is higher than the first air cap (42), and the top of the air inlet partition plate (3) is higher than the second air cap (52).

8. The internal circulation fluidized bed reaction apparatus according to claim 1, characterized by: The heat transfer disturbance unit (8) comprises a heat conduction plate (81) and a disturbance plate (82), the heat conduction plate (81) is fixed on the outer side wall of the reaction shell (1) to transfer heat to the high-speed chamber (11), and a plurality of disturbance plates (82) are distributed side by side along the width direction of the center partition plate (2) in the high-speed chamber (11). One side wall of the disturbance plate (82) is fixed on the inner side wall of the reaction shell (1), and adjacent two disturbance plates (82) form a flow channel for the gas to move upward, and the other side wall of the disturbance plate (82) is in a continuous sinusoidal shape along the vertical direction, and the flow channel forms a periodic contraction section and an expansion section along the vertical direction.

9. The internal circulation fluidized bed reaction apparatus according to claim 1, characterized by: The heat transfer disturbance unit (8) comprises a plurality of electric heating pipes (83) distributed side by side along the width direction of the center partition plate (2) in the high-speed chamber (11), the electric heating pipes (83) are vertically arranged, and the electric heating pipes (83) are in a continuous sinusoidal shape along the vertical direction, and the top end and the bottom end of the electric heating pipes (83) respectively extend out of the reaction shell (1) for connecting with an external power source.

10. The internally circulating fluidized bed reaction apparatus according to claim 1, characterized by: The feeding pipe (6) is located above the first side-inclined partition plate (21), and the feeding pipe (6) is in an inclined structure with the feeding direction inclined toward the low-speed chamber (12), the discharging pipe (7) is located above the air inlet partition plate (3), and the discharging pipe (7) is in an inclined structure with the discharging direction inclined downward, and the top of the reaction shell (1) is further provided with a gas outlet (9).

Images