Multi-zone coupled internal circulation fluidized reactor, hydrogen production system and method from coke tail gas

Abstract

This invention relates to the field of chemical loop hydrogen production technology from semi-coke tail gas, particularly to a multi-zone coupled internal circulation fluidized bed reactor, a semi-coke tail gas hydrogen production system and method. By incorporating three inclined trays within the reactor body, the reactor is divided into an air complete re-oxidation zone, a semi-coke tail gas reduction zone, and a steam oxidation hydrogen production zone. A riser is added to increase the steam-lifted secondary oxidation zone, achieving multi-zone coupling within the same reactor. The semi-coke tail gas reduction zone reduces the oxygen carrier; the steam oxidation hydrogen production zone oxidizes the reduced oxygen carrier to produce hydrogen; the steam-lifted secondary oxidation zone supplements the unreacted oxygen carrier with oxidation and fluidizes it to the air complete re-oxidation zone; and the air complete re-oxidation zone recycles the oxygen carrier, achieving continuous hydrogen production from semi-coke tail gas through chemical looping. This solves the problems of difficult particle-ordered circulation control, insufficient contact time between oxygen carrier particles and the gas phase, and difficulty in continuous and stable hydrogen production in existing semi-coke tail gas chemical loop hydrogen production methods.

Description

Technical Field

[0001] This invention relates to the field of chemical looping hydrogen production technology from semi-coke tail gas, specifically to a multi-zone coupled internal circulation fluidized reactor, a semi-coke tail gas hydrogen production system and method. Background Technology

[0002] Semi-coke production, as a crucial link in the comprehensive utilization of coal, occupies an important position in the energy and chemical industry. Semi-coke is a high-quality solid carbonaceous fuel produced from non-caking or weakly caking bituminous coal through a medium-low temperature dry distillation process. It is characterized by high fixed carbon content, good chemical activity, and low ash and sulfur content, and is widely used in industries such as steel, chemicals, and building materials. The semi-coke production process inevitably generates a certain amount of tail gas. This tail gas typically contains reducing components such as carbon monoxide, hydrogen, and methane, as well as small amounts of tar, sulfides, and dust, possessing high calorific value and resource utilization potential. In current industrial practice, semi-coke tail gas is mostly directly burned for heating or simply recovered as a general low-calorific-value fuel. This utilization method fails to fully exploit the potential value of the reducing components in the semi-coke tail gas and cannot achieve high-value conversion and utilization of the tail gas. With the global pursuit of a low-carbon economy and the urgent need to improve energy efficiency, how to prepare high-purity hydrogen from semi-coke tail gas and achieve high-value conversion and utilization of its reducing components has become an important research topic.

[0003] Currently, various hydrogen production routes have been explored and developed in the industrial sector. A common approach involves a combination of processes including shift conversion, purification, and adsorption separation. This process first involves a shift reaction between carbon monoxide and water vapor in the semi-coke tail gas, using a catalyst to produce carbon dioxide and hydrogen, thus increasing the hydrogen content in the tail gas. Subsequently, the gas after the shift reaction is purified to remove tar, sulfides, dust, and other contaminants. Finally, adsorption separation separates the hydrogen from other gases, yielding hydrogen. While this combined process can produce high-purity hydrogen, it typically suffers from drawbacks such as a long process flow, numerous separation units, complex equipment systems, high energy consumption, and limited stability during continuous operation. Especially when dealing with semi-coke tail gas containing complex components such as methane and tar precursors with significant compositional fluctuations, the conventional process becomes even more reliant on purification and separation units, hindering efficient, stable, and low-load continuous hydrogen production.

[0004] Chemical looping hydrogen production technology, as an emerging method, has gradually attracted attention in recent years. Based on the cyclic oxidation-reduction characteristics of oxygen carriers in different reaction atmospheres, this technology cleverly separates the fuel conversion process from the hydrogen production process. In this technology, fuel first reacts with the oxygen carrier in a reduction reactor, where the fuel is oxidized and the oxygen carrier is reduced. The reduced oxygen carrier then enters an oxidation reactor, where it reacts with water vapor to generate hydrogen, which is then re-oxidized. The oxidized oxygen carrier is then regenerated by air to restore its oxidation capacity, thus completing a full cycle. This unique reaction mechanism gives chemical looping hydrogen production technology many advantages, such as reducing the direct mixing of fuel and air, lowering the risk of explosion; facilitating product diversion and hydrogen purification; and suitability for continuous operation, improving the stability and efficiency of the hydrogen production process. Therefore, chemical looping hydrogen production technology provides a promising new approach for the high-value hydrogen production from semi-coke tail gas, and is expected to overcome the limitations of traditional hydrogen production processes, achieving efficient conversion of reducing components in semi-coke tail gas and high-purity hydrogen production.

[0005] Despite some progress in existing hydrogen production technologies from semi-coke tail gas, several pressing technical challenges remain in practical applications, particularly when dealing with the complex and fluctuating composition of semi-coke tail gas. First, existing technologies often employ conventional series reactors, which typically achieve continuous hydrogen production through gas switching. However, scaling up the reactor size and utilizing heat gradients are difficult, hindering the large-scale and economical aspects of hydrogen production. Second, existing technologies often utilize conventional fluidized bed structures, achieving continuous hydrogen production through particle circulation across multiple reaction spaces. This results in long particle circulation paths, insufficient device integration, and unstable connections between multi-stage reactions. Third, existing particle conveying and return structures primarily function as particle transfer devices, making it difficult for particles to continue participating in effective reactions during the conveying phase. For oxygen carriers that remain in an incompletely oxidized state after the main hydrogen production stage, directly entering the conventional lift-back process hinders further utilization of the oxygen carrier's reaction potential and is detrimental to improving the system's hydrogen production capacity and circulation efficiency. Fourth, in continuous chemical chain reaction systems, the lack of effective gas supply isolation and segmented exhaust design between different reaction zones easily leads to cross-mixing between semi-coke tail gas, reduction tail gas, steam oxidation hydrogen production gas, and air re-oxidation tail gas, affecting the purity of hydrogen production, increasing the burden on subsequent separation, and making it difficult to achieve continuous and stable output of high-purity hydrogen. Fifth, semi-coke tail gas contains reducing components such as methane and may carry small amounts of tar, dust, and sulfide precursors, which places higher demands on the anti-carbon deposition performance of the oxygen carrier, circulation stability, and the gas-solid flow organization mode inside the reactor. If the reaction zone structure design and particle migration path setting are unreasonable, it may also cause problems such as local stagnation, uneven fluidization, limited heat and mass transfer, and poor particle circulation.

[0006] In summary, existing hydrogen production technologies from semi-coke tail gas suffer from numerous technical challenges in reactor design, particle conveying, gas mixing control, and reaction zone structure, severely hindering their efficient, stable, and low-cost development. Therefore, there is an urgent need for a device and method suitable for the continuous chemical looping production of high-purity hydrogen from semi-coke tail gas. This would comprehensively address the aforementioned technical difficulties, promote the industrial application of hydrogen production technologies from semi-coke tail gas, and realize the high-value utilization of semi-coke tail gas resources and the sustainable development of the hydrogen energy industry. Summary of the Invention

[0007] To address the challenges in existing technologies for hydrogen production from semi-coke tail gas, such as difficulties in controlling the orderly circulation of particles, insufficient contact time between oxygen carrier particles and the gas phase, and difficulties in continuous and stable hydrogen production, this invention provides a multi-zone coupled internal circulation fluidized reactor, a semi-coke tail gas hydrogen production system, and a method.

[0008] To achieve the above objectives, the present invention employs the following technical solution: This invention provides a multi-zone coupled internal circulation fluidized bed reactor, including a riser and a body containing an oxygen carrier. The body is provided with a first inclined tray, a second inclined tray, and a third inclined tray from top to bottom. The three inclined trays divide the body into three functional zones, which are, from top to bottom, a complete air re-oxidation zone, a semi-coke tail gas reduction zone, and a steam oxidation hydrogen production zone. The first inclined tray, the second inclined tray, and the third inclined tray are all provided with particle channels to connect two adjacent functional zones. The first, second, and third inclined trays are each provided with a high-speed gas inlet and a low-speed gas inlet for introducing the required gas into the corresponding functional areas. The high-speed gas inlet is located on the lower inclined side of the inclined tray, and the low-speed gas inlet is located on the upper inclined side of the inclined tray. The upper inclined side is the higher side of the inclined tray, and the lower inclined side is the lower side of the inclined tray. The complete air re-oxidation zone is used to introduce air to completely re-oxidize the oxygen carrier, and the complete air re-oxidation zone is provided with an air re-oxidation exhaust gas outlet. The semi-coke tail gas reduction zone is used to introduce semi-coke tail gas to reduce the oxygen carrier, and the semi-coke tail gas reduction zone is provided with a reduction tail gas outlet. The steam oxidation hydrogen production zone is used to introduce steam to oxidize the reduced oxygen carrier to produce hydrogen, and the steam oxidation hydrogen production zone is provided with a first hydrogen outlet. One end of the riser is connected to the air complete re-oxidation zone, and the other end is provided with a steam riser chamber. The steam riser chamber and the steam oxidation hydrogen production zone are connected through a particle channel set on the third inclined tower plate to form a steam riser secondary oxidation zone. The steam-lift secondary oxidation zone is used to introduce water vapor to supplement the oxidation of the oxygen carrier to produce hydrogen and to fluidize and lift the oxygen carrier to the air complete re-oxidation zone. The steam-lift secondary oxidation zone is provided with a second hydrogen outlet.

[0009] Optionally, the particle channels are respectively disposed on the downward inclined side of the first inclined tray, the second inclined tray, and the third inclined tray, and the inlet height of the particle channels is higher than the height of the lowest point of the inclined slope of the oxygen carrier on the corresponding inclined tray.

[0010] Optionally, elbows are provided at the outlets of the particle channels on the first and second inclined trays.

[0011] Optionally, the outlet of the particle channel located on the downward side of the third inclined tray is connected to the steam-lifted secondary oxidation zone via a valve port.

[0012] Optionally, a cyclone tube is provided at the connection between the steam-lift secondary oxidation zone and the air complete re-oxidation zone, and the second hydrogen outlet is located at the top gas outlet of the cyclone tube, with the oxygen carrier entering the air complete re-oxidation zone through the bottom of the cyclone tube.

[0013] Optionally, the tilting directions of two adjacent tilted trays are opposite.

[0014] Optionally, the body is a hollow cylindrical structure or a cuboid structure.

[0015] The present invention also provides a hydrogen production system from semi-coke tail gas, including an air heater, a steam heater, and a semi-coke tail gas pretreatment device, a blower, a raw material preheater, a raw material gas heater, and the above-mentioned multi-zone coupled internal circulation fluidized reactor connected in sequence to the semi-coke tail gas outlet. The outlet of the raw material gas heater is connected to the high-speed gas inlet and the low-speed gas inlet provided on the second inclined tower plate; The air heater has an inlet connected to an air source and an outlet connected to a high-speed gas inlet and a low-speed gas inlet on the first inclined tower plate. The inlet of the steam heater is connected to a steam source, and the outlet of the steam heater is connected to the inlet of the steam lifting chamber and the high-speed gas inlet and low-speed gas inlet on the third inclined tower plate.

[0016] Optionally, the system also includes a gas cooler, the inlet of which is connected to a first hydrogen outlet and a second hydrogen outlet, and the outlet of which is connected to a hydrogen storage device.

[0017] The present invention also provides a method for producing hydrogen from semi-coke tail gas using the above-mentioned multi-zone coupled internal circulation fluidized reactor, comprising: After the purified semi-coke tail gas is heated, it is introduced into the semi-coke tail gas reduction zone through the high-speed gas inlet and the low-speed gas inlet on the second inclined tower plate, respectively, in the form of high-speed semi-coke tail gas and low-speed semi-coke tail gas. The oxygen carrier reacts with the high-speed semi-coke tail gas and is blown up by the high-speed semi-coke tail gas. A portion falls into the low-speed semi-coke tail gas zone and reacts with the low-speed semi-coke tail gas, and is circulated back to the high-speed semi-coke tail gas zone under the action of the second inclined tower plate; the other portion falls into the water vapor oxidation hydrogen production zone along the particle channel; wherein, the low-speed semi-coke tail gas zone is the area corresponding to the low-speed gas inlet on the second inclined tower plate, and the high-speed semi-coke tail gas zone is the area corresponding to the high-speed gas inlet on the second inclined tower plate. The reducing tail gas generated after the oxygen carrier reacts with the heated semi-coke tail gas is discharged through the reducing tail gas outlet. Part of the heated steam is introduced into the steam oxidation hydrogen production zone through the high-speed gas inlet and low-speed gas inlet of the third inclined tray, respectively, in the form of high-speed steam and low-speed steam; the other part enters the steam lifting secondary oxidation zone through the steam lifting chamber. The oxygen carrier, after reacting with the semi-coke tail gas in the steam oxidation hydrogen production zone, is then reacted with high-speed steam and blown up by the high-speed steam. Part of it falls into the low-speed steam zone to react with the low-speed steam to produce hydrogen, and is then recycled to the high-speed steam zone under the action of the third tilted tray. The other part falls along the particle channel into the steam lifting secondary oxidation zone. The low-speed steam zone is the area corresponding to the low-speed gas inlet on the third tilted tray, and the high-speed steam zone is the area corresponding to the high-speed gas inlet on the third tilted tray. The hydrogen produced in the steam oxidation hydrogen production zone is discharged through the first hydrogen outlet and stored after gas-water separation. The oxygen carrier that has fallen into the steam lifting secondary oxidation zone and reacted with water vapor is lifted along the steam lifting secondary oxidation zone to the air complete re-oxidation zone under the action of water vapor introduced into the steam lifting chamber. At the same time, it continues to react with the oxygen carrier that has not completely reacted in the water vapor oxidation hydrogen production zone to produce hydrogen. The hydrogen produced by the steam lifting secondary oxidation zone is discharged through the second hydrogen outlet, and then stored after gas-liquid separation. The heated air is introduced into the air re-oxidation zone through the high-speed gas inlet and the low-speed gas inlet on the first inclined tower plate, respectively, in the form of high-speed air and low-speed air. The oxygen carrier, which is lifted by water vapor to the air re-oxidation zone, reacts with high-speed air and is blown up by the high-speed air. Part of it falls into the low-speed air zone to react with low-speed air and is then circulated to the high-speed air zone under the action of the first tilted tower plate. The other part falls along the particle channel into the semi-coke tail gas reduction zone to react with semi-coke tail gas and participate in the next semi-coke tail gas hydrogen production cycle. The low-speed air zone is the area corresponding to the low-speed gas inlet on the first tilted tower plate, and the high-speed air zone is the area corresponding to the high-speed gas inlet on the first tilted tower plate. The re-oxidation tail gas generated after the oxygen carrier reacts with heated air is discharged through the air re-oxidation tail gas outlet, completing a hydrogen production cycle from semi-coke tail gas.

[0018] Compared with the prior art, the present invention has the following beneficial effects: This invention provides a multi-zone coupled internal circulation fluidized bed reactor. The reactor is divided into an air complete re-oxidation zone, a semi-coke tail gas reduction zone, and a steam oxidation hydrogen production zone by three inclined trays inside the reactor body. A secondary oxidation zone is added via a riser, achieving multi-zone coupling within the same reactor. The semi-coke tail gas reduction zone uses the semi-coke tail gas to reduce the oxygen carrier. The steam oxidation hydrogen production zone oxidizes the reduced oxygen carrier to produce hydrogen. The secondary oxidation zone replenishes unreacted oxygen carriers and fluidizes them to the air complete re-oxidation zone. The oxygen carriers are then re-oxidized and recycled for hydrogen production from the semi-coke tail gas within the air complete re-oxidation zone. This achieves chemical looping hydrogen production from semi-coke tail gas within the same reactor. Compared to traditional independent series chemical looping reactors, this method features a simple and compact structure, small footprint, low heat loss, short oxygen carrier circulation path, low circulation energy consumption, and low investment cost. Simultaneously, by setting up three inclined trays with a low-velocity gas inlet on the inclined side of the tray and a high-velocity gas inlet on the downward-inclined side, the high-velocity gas inlet allows for the upward movement of oxygen carrier particles and promotes inter-zone transport. The low-velocity gas inlet allows for the flow of lower-velocity gas to maintain bed stability and prevent particle accumulation. Under the tilting action of the inclined trays, the gas flows towards the high-velocity gas inlet, thus forming a local internal circulation. This allows the oxygen carrier to fully react with the gas in the corresponding functional area, while simultaneously completing the processes of semi-coke tail gas reduction, steam oxidation for hydrogen production, steam lifting secondary oxidation, and complete air re-oxidation along a predetermined particle path within the reactor. This enables multiple reaction stages to be sequentially connected within the same continuous system. Compared to traditional semi-coke tail gas hydrogen production reactors, this method achieves sequential and active transfer of oxygen carrier particles, allowing the oxygen carrier to continue participating in the reaction during the transport stage. This further taps into the reaction potential of the oxygen carrier, improves its utilization rate, and ultimately enhances the system's hydrogen production capacity and circulation efficiency. Finally, by setting corresponding gas outlets in each functional area, the reaction gases in each zone are preferentially discharged along their respective exhaust channels, reducing direct mixing of different reaction atmospheres inside the reactor and achieving continuous and stable output of high-purity hydrogen. Compared with traditional semi-coke tail gas hydrogen production reactors, this design reduces the mixing of impurities at the source, and the subsequent acquisition of high-purity hydrogen does not rely on complex end-of-pipe purification; high-purity hydrogen can be further obtained simply through condensation and dehydration, further reducing hydrogen production costs. The reactor has a simple structure, with optimized design of only three inclined trays, a few gas inlets and outlets, a few particle channels, and risers. This design allows for controlled particle migration between different functional zones while achieving maximum isolation in the gas path, thus balancing enhanced gas-solid contact, stable particle circulation, and continuous output of high-purity hydrogen. Furthermore, the multi-zone coupling and flow guiding structure helps mitigate the carbon deposition caused by reducing components such as methane, enhances the stability of the oxygen carrier circulation, and improves the long-term operating capability of the unit. It has broad application prospects in the resource utilization of semi-coke tail gas.

[0019] The particle channel is located on the downward tilted side of the inclined tray, and the inlet height of the particle channel is higher than the height of the lowest point of the inclined slope of the oxygen carrier on the corresponding inclined tray. This can prevent a large number of oxygen carrier particles from entering the next area too early, thereby improving the utilization rate of the oxygen carrier.

[0020] Both the particle channels on the first and second inclined trays have elbows at their outlets. This allows oxygen-carrying particles that have passed through the previous zone to fall directly into the current zone via the elbows. After reacting with the gas introduced into the current zone, they participate in the circulation within the zone, preventing the oxygen-carrying particles from directly entering the next zone and ensuring the effective reaction of the oxygen-carrying material.

[0021] The outlet of the particle channel located on the lower side of the third inclined tray is connected to the steam-lifting secondary oxidation zone via a valve. The valve allows the particle channel on the lower side of the third inclined tray to form a channel structure with a turning and lifting function, similar to an L-shaped channel. This balances the lifting of oxygen-carrying particles, the stabilization of return material, and the steam replenishment reaction, ensuring the stability of the oxygen-carrying particle circulation and the sufficiency of the reaction.

[0022] The cyclone tube can separate the lifted oxygen carrier particles from the generated gas, allowing the oxygen carrier particles to enter the air complete re-oxidation zone downwards or tangentially along the cyclone tube wall, while the generated hydrogen gas is discharged through the second hydrogen gas outlet in the center of the cyclone tube, thus forming a gas seal at the connection point. This significantly reduces gas cross-contamination between the vapor-lifted secondary oxidation zone and the air complete re-oxidation zone, ensuring the atmosphere purity of each functional area.

[0023] The two adjacent tilted trays are tilted in opposite directions so that the oxygen carrier can fall from the downward tilt side of the upper tilted tray to the upward tilt side of the lower tilted tray, and then rely on gravity to traverse the entire tilted tray in the opposite direction to participate in the circulation within this area.

[0024] The main body is a hollow cylindrical or cuboid structure, which facilitates the layout of tilting trays and various gas inlets and outlets, and has low manufacturing cost.

[0025] This invention discloses a hydrogen production system from semi-coke tail gas, comprising the aforementioned multi-zone coupled internal circulation fluidized bed reactor, including the aforementioned multi-zone coupled internal circulation fluidized bed reactor, an air heater, a steam heater, and a semi-coke tail gas pretreatment device, a blower, a raw material preheater, and a raw material gas heater connected in sequence to the semi-coke tail gas outlet; the system configures independent gas heating and conveying lines for the three functional zones of the multi-zone coupled internal circulation fluidized bed reactor: the air complete re-oxidation zone, the semi-coke tail gas reduction zone, and the steam oxidation hydrogen production zone, so that the semi-coke tail gas, steam, and air do not interfere with each other, ensuring that the oxygen carrier undergoes the expected reaction in its respective zone.

[0026] The gas cooler can cool the gases output from the first and second hydrogen outlets to below the water vapor dew point, causing the water to condense into liquid water and separate, directly obtaining dry, high-purity hydrogen without relying on complex end-stage purification processes. At the same time, while cooling the hydrogen, the gas cooler can recover the latent heat of condensation of water vapor for preheating semi-coke tail gas, water, or air, thereby reducing external energy input and improving the energy utilization efficiency of the entire system.

[0027] This invention also provides a method for producing hydrogen from semi-coke tail gas using the aforementioned multi-zone coupled internal circulation fluidized bed reactor. This method strictly defines the circulation path of the oxygen carrier in the semi-coke tail gas reduction zone, the steam oxidation hydrogen production zone, the steam lifting secondary oxidation zone, and the air complete re-oxidation zone. This ensures that the four stages of oxygen carrier reduction, hydrogen production, gas replenishment for hydrogen production, and re-oxidation are seamlessly connected in time and space, forming a closed loop. This allows the multi-zone coupled internal circulation characteristics of the reactor to be fully utilized, achieving efficient and continuous hydrogen production. At the same time, it has the advantages of being simple and easy to control, and can effectively promote the industrialization of semi-coke tail gas chemical loop hydrogen production technology. Attached Figure Description

[0028] Figure 1 This is a schematic diagram of a multi-zone coupled internal circulation fluidized reactor provided for Embodiment 1 of the present invention.

[0029] Figure 2 This is a schematic diagram of a multi-zone coupled internal circulation fluidized reactor provided for Embodiment 2 of the present invention.

[0030] Figure 3 The diagram below shows a hydrogen production system based on semi-coke tail gas, provided in Embodiment 3 of the present invention.

[0031] Figure 4 This is a schematic diagram of a hydrogen production method from semi-coke tail gas provided in Embodiment 4 of the present invention.

[0032] Among them, 1-body, 2-first inclined tray, 3-second inclined tray, 4-third inclined tray, 5-oxygen carrier, 6-high-speed gas inlet, 7-low-speed gas inlet, 8-air re-oxidation tail gas outlet, 9-reduction tail gas outlet, 10-first hydrogen outlet, 11-particle channel, 12-riser pipe, 13-steam riser chamber, 14-steam riser inlet, 15-second hydrogen outlet, 16-cyclone pipe, 17-elbow, 18-valve port, 19-semi-coke tail gas pretreatment device, 20-fan, 21-raw material preheater, 22-raw material gas heater, 23-steam heater, 24-air heater, 25-gas cooler, 26-multi-zone coupled internal circulation fluidized reactor. Detailed Implementation

[0033] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The components of the embodiments of the present invention described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0034] Therefore, the following detailed description of the embodiments of the invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the invention without inventive effort are within the scope of protection of the invention.

[0035] It should be noted that similar labels and letters in the following figures indicate similar items. Therefore, once an item is defined in one figure, it does not need to be further defined and explained in subsequent figures.

[0036] In the description of the embodiments of the present invention, it should be noted that if terms such as "upper," "lower," "horizontal," or "inner" indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship commonly used when the product of the invention is in use, they are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the present invention. Furthermore, terms such as "first" and "second" are only used to distinguish descriptions and should not be construed as indicating or implying relative importance.

[0037] Furthermore, the use of the term "horizontal" does not imply that the component must be absolutely horizontal, but rather that it can be slightly tilted. For example, "horizontal" simply means that its direction is more horizontal than "vertical," and does not mean that the structure must be completely horizontal, but can be slightly tilted.

[0038] In the description of the embodiments of the present invention, it should also be noted that, unless otherwise explicitly specified and limited, the terms "set," "install," "connect," and "link" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in the present invention according to the specific circumstances.

[0039] The present invention will be further described in detail below with reference to specific embodiments. These descriptions are for explanation purposes only and are not intended to limit the scope of the invention.

[0040] Example 1 See Figure 1 The present invention discloses a multi-zone coupled internal circulation fluidized reactor, including a body 1 and a riser 12 connected to the body 1; The body 1 is a hollow cuboid structure, and the body 1 is filled with an oxygen carrier 5. Preferably, the oxygen carrier 5 is an iron-aluminum based composite oxygen carrier with anti-carbon deposition ability and cycle stability, and more preferably an Fe-Al composite oxygen carrier or a FeAl2O4 based oxygen carrier. The main body 1 is provided with a first inclined tray 2, a second inclined tray 3, and a third inclined tray 4 arranged sequentially from top to bottom. Each of the first inclined tray 2, the second inclined tray 3, and the third inclined tray 4 is provided with a high-speed gas inlet 6 and a low-speed gas inlet 7. The high-speed gas inlet 6 is located on the lower inclined side of the inclined tray, and the low-speed gas inlet 7 is located on the upper inclined side of the inclined tray. The inclination angle of the inclined tray can be determined according to the friction angle of the oxygen carrier 5. Preferably, the static stacking angle of the oxygen carrier 5 particles is 30°, and the inclination angle of the inclined tray can be set to 35-45°. For oxygen carrier 5 particles with good flowability, the stacking angle can be as small as 15-20°, and the preferred inclination angle of the inclined tray is 25-35°.

[0041] The area between the first inclined tower plate 2 and the top of the body 1 is an air complete re-oxidation zone, which is used for the complete re-oxidation of the oxygen carrier 5. The body 1 of the air complete re-oxidation zone is provided with an air re-oxidation tail gas outlet 8. The area between the first inclined tower plate 2 and the second inclined tower plate 3 is a semi-coke tail gas reduction zone, which is used to introduce semi-coke tail gas to reduce the oxygen carrier 5. The main body 1 of the semi-coke tail gas reduction zone is provided with a reduction tail gas outlet 9. The area between the second inclined tray 3 and the third inclined tray 4 is a steam oxidation hydrogen production zone, which is used to introduce steam to oxidize the reduced oxygen carrier 5 to produce hydrogen. The main body 1 of the steam oxidation hydrogen production zone is provided with a first hydrogen outlet 10. The riser pipe 12 is located on one side of the main body 1. One end of the riser pipe 12 is connected to the air complete re-oxidation zone, and the other end is provided with a steam riser chamber 13. A steam riser inlet 14 is provided on the steam riser chamber 13. The area between the steam riser chamber 13 and the air complete re-oxidation zone in the riser pipe 12 is a steam riser secondary oxidation zone, which is used to introduce steam to supplement the oxygen carrier 5 that has not been completely oxidized and fluidized to the air complete re-oxidation zone. A second hydrogen outlet 15 is provided on the riser pipe 12 of the steam riser secondary oxidation zone. A vortex tube 16 is provided at the connection between the riser pipe 12 and the air complete re-oxidation zone. The second hydrogen outlet 15 is provided on the vortex tube 16. The air complete re-oxidation zone, the semi-coke tail gas reduction zone, the steam oxidation hydrogen production zone, and the steam rise secondary oxidation zone are sequentially connected by a particle channel 11. The particle channels 11 are respectively located on the downward-sloping sides of the first inclined tray 2, the second inclined tray 3, and the third inclined tray 4, and the inlet height of the particle channel 11 is higher than the height of the lowest point of the inclined slope of the oxygen carrier 5 on the corresponding inclined tray. The outlets of the particle channels 11 located on the first inclined tray 2 and the second inclined tray 3 are each equipped with elbows 17; the outlet of the particle channel 11 located on the downward-sloping side of the third inclined tray 4 is connected to the steam rise secondary oxidation zone via a valve port 18. Preferably, the inclination directions of two adjacent inclined trays are opposite.

[0042] The gas velocities of the high-speed gas inlet 6 and the low-speed gas inlet 7 are related to the particle density, diameter, and sphericity. The gas flow rate of the high-speed gas inlet 6 needs to be sufficient to blow up the oxygen carrier 5 particles. The blowing height should be such that some of the oxygen carrier 5 particles fall into the area corresponding to the low-speed gas inlet 7, and some fall into the next area. In this embodiment, the gas flow rate of the low-speed gas inlet 7 is set to 1.2-2 times the minimum fluidization velocity, and the gas flow rate of the high-speed gas inlet 6 is 3.5-5 times the minimum fluidization velocity.

[0043] This multi-zone coupled internal circulation fluidized bed reactor constructs a particle circulation path that combines steam lifting and secondary oxidation. The newly added steam lifting secondary oxidation zone enables the oxygen carrier 5 to not only be lifted and transported during its migration from the steam oxidation hydrogen production zone to the air complete re-oxidation zone, but also to continue reacting with supplementary steam, thereby improving the utilization rate of the oxygen carrier 5 and the reactor's hydrogen production capacity. Through the layered or partitioned arrangement of functional zones, directional particle circulation, and independent supply and exhaust channels, cross-mixing between different reaction atmospheres can be reduced, providing structural assurance for continuous output of high-purity hydrogen from the source and reducing the complexity of subsequent separation processes.

[0044] Example 2 See Figure 2 The present invention discloses a multi-zone coupled internal circulation fluidized reactor, including a body 1, wherein the body 1 is a hollow cylindrical structure, and the body 1 is filled with an oxygen carrier 5. Preferably, the oxygen carrier 5 is an iron-aluminum based composite oxygen carrier with anti-carbon deposition ability and circulation stability, and more preferably an Fe-Al composite oxygen carrier or a FeAl2O4 based oxygen carrier. The main body 1 is provided with a riser pipe 12. In the cavity between the riser pipe 12 and the main body 1, a first inclined tower plate 2, a second inclined tower plate 3 and a third inclined tower plate 4 are arranged sequentially from top to bottom. The first inclined tower plate 2, the second inclined tower plate 3 and the third inclined tower plate 4 are each provided with a high-speed gas inlet 6 and a low-speed gas inlet 7. The high-speed gas inlet 6 is located on the lower inclined side of the inclined tower plate and the low-speed gas inlet 7 is located on the upper inclined side of the inclined tower plate. The area between the first inclined tower plate 2 and the top of the body 1 is an air complete re-oxidation zone, which is used for the complete re-oxidation of the oxygen carrier 5. The body 1 of the air complete re-oxidation zone is provided with an air re-oxidation tail gas outlet 8. The area between the first inclined tower plate 2 and the second inclined tower plate 3 is a semi-coke tail gas reduction zone, which is used to introduce semi-coke tail gas to reduce the oxygen carrier 5. The main body 1 of the semi-coke tail gas reduction zone is provided with a reduction tail gas outlet 9. The area between the second inclined tray 3 and the third inclined tray 4 is a steam oxidation hydrogen production zone, which is used to introduce steam to oxidize the reduced oxygen carrier 5 to produce hydrogen. The main body 1 of the steam oxidation hydrogen production zone is provided with a first hydrogen outlet 10. One end of the riser pipe 12 is connected to the air complete re-oxidation zone, and the other end is provided with a steam riser chamber 13. A steam riser inlet 14 is provided on the steam riser chamber 13. The area between the steam riser chamber 13 and the air complete re-oxidation zone in the riser pipe 12 is a steam riser secondary oxidation zone, which is used to introduce steam to supplement the oxygen carrier 5 that has not been completely oxidized and fluidize and lift it to the air complete re-oxidation zone. A second hydrogen outlet 15 is provided on the riser pipe 12 of the steam riser secondary oxidation zone. A swirl tube 16 is provided at the connection between the riser pipe 12 and the air complete re-oxidation zone. The second hydrogen outlet 15 is provided on the swirl tube 16. The air complete re-oxidation zone, the semi-coke tail gas reduction zone, the steam oxidation hydrogen production zone, and the steam rise secondary oxidation zone are sequentially connected by a particle channel 11. The particle channels 11 are respectively located on the downward-sloping sides of the first inclined tray 2, the second inclined tray 3, and the third inclined tray 4, with the inlet height of the particle channel 11 higher than the lowest point of the inclined slope of the oxygen carrier 5 on the corresponding inclined tray. Elbows 17 are provided at the outlets of the particle channels 11 located on the first inclined tray 2 and the second inclined tray 3. The outlet of the particle channel 11 located on the downward-sloping side of the third inclined tray 4 is connected to the steam rise secondary oxidation zone via a valve port 18. Preferably, the first inclined tray 2 and the second inclined tray 3 are inclined in opposite directions, and the downward-sloping side of the fourth inclined tray 4 is connected to the outer peripheral wall of the riser pipe 12. Preferably, the high-speed gas inlet 6 and low-speed gas inlet 7 that supply gas to the steam oxidation hydrogen production zone can be set to multiple locations to adapt to the fluidization enhancement requirements under different hydrogen production load conditions; preferably, the particle channel 11 connected to the fourth inclined tray 4 is connected to the steam oxidation hydrogen production zone through the valve port 18 to form an L-shaped channel or a channel structure with deflection and lifting function, so as to take into account particle lifting, return material stabilization and steam replenishment reaction.

[0045] The reaction process of the oxygen carrier 5 in the multi-zone coupled internal circulating fluidized reactor is as follows: In the semi-coke tail gas reduction zone, the oxidized oxygen carrier 5 comes into contact with the pretreated and heated semi-coke tail gas and undergoes a reduction reaction to form a reduced or partially reduced oxygen carrier 5. The generated reduced tail gas is discharged through the reduced tail gas outlet 9 corresponding to the semi-coke tail gas reduction zone. The reduced or partially reduced oxygen carrier 5 is blown up by the semi-coke tail gas entering through the high-speed gas inlet 6. A portion of it falls into the semi-coke tail gas reduction zone corresponding to the low-speed gas inlet 7 and continues to come into contact with the semi-coke tail gas for reduction, forming a local circulation within the semi-coke tail gas reduction zone. Under the action of the second inclined tower plate 3, it continues to circulate and is blown up by the semi-coke tail gas entering through the high-speed gas inlet 6, falling into the water vapor oxidation hydrogen production zone through the particle channel 11.

[0046] In the steam oxidation hydrogen production zone, the reduced oxygen carrier 5 particles come into contact with heated steam to undergo an oxidation reaction and generate hydrogen gas, which is then output and stored through the first hydrogen outlet 10. At the same time, the oxygen carrier 5, after participating in the oxidation reaction, is blown up by the steam entering through the high-speed gas inlet 6 and circulates in the steam oxidation hydrogen production zone to undergo an oxidation reaction. In each cycle, a portion of the oxygen carrier 5 falls into the steam lifting secondary oxidation zone through the particle channel 11.

[0047] In the steam-lifting secondary oxidation zone, the oxygen carrier 5 particles, after completing the main hydrogen production reaction, are further oxidized by the supplementary steam after entering the steam-lifting chamber 13 through the steam-lifting inlet 14, and then fluidized along the lift pipe 12. During the fluidized lifting process, the incompletely oxidized oxygen carrier 5 continues to react with the supplementary steam to produce hydrogen, which is then discharged and stored through the second hydrogen outlet 15. Thus, this zone simultaneously achieves the two functions of oxygen carrier 5 particle lifting and return and supplementary oxidation.

[0048] After secondary oxidation by steam lifting, the oxygen carrier particles 5 enter the air re-oxidation zone through the cyclone tube 16. There, they undergo a re-oxidation reaction with the incoming air and participate in the regional circulation within the air re-oxidation zone. Once restored to their oxidized state, the oxygen carrier particles 5 return to the semi-coke tail gas reduction zone, completing the closed-loop circulation of the oxygen carrier particles 5. The air re-oxidation tail gas generated in the air re-oxidation zone is discharged through the air re-oxidation tail gas outlet 8.

[0049] Example 3 See Figure 3 The present invention also provides a hydrogen production system from semi-coke tail gas, including a gas cooler 25, an air heater 24, a steam heater 23, and a semi-coke tail gas pretreatment device 19, a fan 20, a raw material preheater 21, a raw material gas heater 22, and the above-mentioned multi-zone coupled internal circulation fluidized reactor 26 connected in sequence to the semi-coke tail gas outlet. The semi-coke tail gas pretreatment device 19 is used to remove dust, desulfurize, and remove tar or impurities from the semi-coke tail gas to reduce the impact of impurities on the activity of the oxygen carrier 5 and the continuous operation stability of the multi-zone coupled internal circulation fluidized reactor 26. The fan 20, raw material preheater 21, air heater 24, steam heater 23, and raw material gas heater 22 are used to provide semi-coke tail gas, steam, and air that meet the reaction conditions to the multi-zone coupled internal circulation fluidized reactor 26; the gas cooler 25 is used to condense and dehydrate the hydrogen produced in the steam oxidation hydrogen production zone and the steam lifting secondary oxidation zone to obtain high-purity hydrogen. Preferably, the gas cooler 25 is connected to a gas-liquid separator. The outlet of the raw material gas heater 22 is connected to the high-speed gas inlet 6 and the low-speed gas inlet 7 provided on the second inclined tower plate 3; The air heater 24 is connected to an air source at its inlet and to a gas high-speed inlet 6 and a gas low-speed inlet 7 on the first inclined tower plate 2 at its outlet. The inlet of the steam heater 23 is connected to a steam source, and the outlet of the steam heater 23 is connected to the steam lifting inlet 14 and the high-speed gas inlet 6 and the low-speed gas inlet 7 on the third inclined tower plate 4. The inlet of the gas cooler 25 is connected to the first hydrogen outlet 10 and the second hydrogen outlet 15, and the outlet of the gas cooler 25 is connected to a hydrogen storage device.

[0050] Example 4 See Figure 4 The present invention also provides a method for producing hydrogen from semi-coke tail gas using the above-mentioned multi-zone coupled internal circulation fluidized reactor, comprising: After the purified semi-coke tail gas is heated, it is introduced into the semi-coke tail gas reduction zone through the high-speed gas inlet 6 and the low-speed gas inlet 7 on the second inclined tower plate 3, respectively, in the form of high-speed semi-coke tail gas and low-speed semi-coke tail gas. The oxygen carrier 5 reacts with the high-speed semi-coke tail gas and is blown up by the high-speed semi-coke tail gas. Part of it falls into the low-speed semi-coke tail gas zone and reacts with the low-speed semi-coke tail gas, and is circulated back to the high-speed semi-coke tail gas zone under the action of the second inclined tower plate 3; the other part falls into the water vapor oxidation hydrogen production zone along the particle channel 11. The low-speed semi-coke tail gas zone is the area corresponding to the low-speed gas inlet 7 on the second inclined tower plate 3, and the high-speed semi-coke tail gas zone is the area corresponding to the high-speed gas inlet 6 on the second inclined tower plate 3. The reducing tail gas generated after the oxygen carrier 5 reacts with the heated semi-coke tail gas is discharged through the reducing tail gas outlet 9. Part of the heated steam is introduced into the steam oxidation hydrogen production zone through the high-speed gas inlet 6 and the low-speed gas inlet 7 of the third inclined tower plate 4, respectively, in the form of high-speed steam and low-speed steam; the other part enters the steam lifting secondary oxidation zone through the steam lifting chamber 13. The oxygen carrier 5, after reacting with the semi-coke tail gas in the steam oxidation hydrogen production zone, reacts with high-speed steam and is blown up by the high-speed steam. Part of it falls into the low-speed steam zone to react with low-speed steam to produce hydrogen, and is then recycled to the high-speed steam zone under the action of the third tilted tray 4; the other part falls along the particle channel 11 into the steam lifting secondary oxidation zone. The low-speed steam zone is the area corresponding to the low-speed gas inlet 7 on the third tilted tray 4, and the high-speed steam zone is the area corresponding to the high-speed gas inlet 6 on the third tilted tray 4. The hydrogen produced in the steam oxidation hydrogen production zone is discharged through the first hydrogen outlet 10 and stored after gas-water separation. The oxygen carrier 5, which has reacted with water vapor after falling into the steam lifting secondary oxidation zone, is lifted along the steam lifting secondary oxidation zone to the air complete re-oxidation zone under the action of water vapor introduced into the steam lifting chamber 13. At the same time, it continues to react with the oxygen carrier 5 that has not completely reacted in the steam oxidation hydrogen production zone to produce hydrogen. The hydrogen produced by the steam lifting secondary oxidation zone is discharged through the second hydrogen outlet 15 and stored after gas-liquid separation. The heated air is introduced into the air re-oxidation zone through the high-speed gas inlet 6 and the low-speed gas inlet 7 on the first inclined tower plate 2, respectively, in the form of high-speed air and low-speed air. The oxygen carrier 5, which is lifted by water vapor to the air re-oxidation zone, reacts with high-speed air and is blown up by the high-speed air. Part of it falls into the low-speed air zone and reacts with low-speed air, and is then circulated to the high-speed air zone under the action of the first tilted tower plate 2. The other part falls along the particle channel 11 into the semi-coke tail gas reduction zone and reacts with the semi-coke tail gas, participating in the next semi-coke tail gas hydrogen production cycle. The low-speed air zone is the area corresponding to the low-speed gas inlet 7 on the first tilted tower plate 2, and the high-speed air zone is the area corresponding to the high-speed gas inlet 6 on the first tilted tower plate 2. The re-oxidation tail gas generated after the oxygen carrier 5 reacts with heated air is discharged through the air re-oxidation tail gas outlet 8, completing a semi-coke tail gas hydrogen production cycle.

[0051] Preferably, the reaction temperature of the semi-coke tail gas reduction zone and the steam oxidation hydrogen production zone is above 700°C. In actual operation, the gas flow rate can be controlled by setting control valves at the high-speed gas inlet 6 and the low-speed gas inlet 7, or the gas flow rate entering the high-speed gas inlet 6 and the low-speed gas inlet 7 can be controlled by dividing the gas output process into high-speed and low-speed pipelines.

[0052] This method strictly defines the cyclic path of the oxygen carrier in the semi-coke tail gas reduction zone, the steam oxidation hydrogen production zone, the steam lifting secondary oxidation zone, and the air complete re-oxidation zone. This ensures that the four stages of oxygen carrier 5—reduction, hydrogen production, gas replenishment for hydrogen production, and re-oxidation—are seamlessly connected in time and space, forming a closed loop and achieving efficient and continuous hydrogen production.

[0053] In summary, this invention provides a multi-zone coupled internal circulation fluidized bed reactor, a semi-coke tail gas hydrogen production system and method. The multi-zone coupled internal circulation fluidized bed reactor 26 integrates the semi-coke tail gas reduction zone, the steam oxidation hydrogen production zone, the steam lift secondary oxidation zone, and the air complete re-oxidation zone into the same reactor, which is beneficial for shortening the particle circulation path, strengthening gas-solid contact, and improving the compactness and stability of continuous operation of the device. By setting up the steam lift secondary oxidation zone, the oxygen carrier 5 particles continue to participate in the oxidation reaction during the lifting and conveying process, no longer just a simple return material conveying process, but a supplementary oxidation of the unreacted oxygen carrier 5 during the return material conveying process, improving the further utilization of the incompletely oxidized oxygen carrier 5 particles, and enhancing the recycling efficiency of the oxygen carrier 5. By employing independent gas supply and exhaust for each functional area, along with a directional circulation system for the oxygen carrier 5 particles, the risk of cross-contamination between reduction tail gas, hydrogen, and re-oxidation tail gas is effectively reduced. This improves hydrogen purity from the source, providing a structural foundation for continuous high-purity hydrogen output. Subsequent high-purity hydrogen products can be obtained simply through condensation and dehydration, reducing the complexity of traditional multi-stage separation and purification processes. Furthermore, this invention utilizes an iron-aluminum based composite oxygen carrier adapted to the complex composition of semi-coke tail gas, coupled with a multi-zone coupling structure. This helps mitigate the carbon deposition caused by reducing components such as methane, enhancing the circulation stability of the oxygen carrier 5 and the long-term operational capability of the device. This provides a possibility for promoting the industrial application of hydrogen production technology from semi-coke tail gas, realizing the high-value utilization of semi-coke tail gas resources, and achieving sustainable development of the hydrogen energy industry.

[0054] The above description is merely a preferred embodiment of the present invention and is not intended to limit the technical solution of the present invention in any way. Those skilled in the art should understand that, without departing from the spirit and principles of the present invention, the technical solution can be modified and replaced in several simple ways, and these modifications and replacements are all within the scope of protection covered by the claims.

Claims

1. A multi-zone coupled internal circulation fluidized bed reactor, characterized in that, The system includes a riser (12) and a body (1) containing an oxygen carrier (5). The body (1) is provided with a first inclined tower plate (2), a second inclined tower plate (3), and a third inclined tower plate (4) from top to bottom. The three inclined tower plates divide the body (1) into three functional areas, which are, from top to bottom, the air complete re-oxidation zone, the semi-coke tail gas reduction zone, and the water vapor oxidation hydrogen production zone. The first inclined tower plate (2), the second inclined tower plate (3), and the third inclined tower plate (4) are all provided with particle channels (11) to connect two adjacent functional areas. The first tilted tower plate (2), the second tilted tower plate (3) and the third tilted tower plate (4) are each provided with a high-speed gas inlet (6) and a low-speed gas inlet (7) for introducing the required gas into the corresponding functional area; the high-speed gas inlet (6) is located on the lower tilted side of the tilted tower plate and the low-speed gas inlet (7) is located on the upper tilted side of the tilted tower plate. The air complete reoxidation zone is used to introduce air so that the oxygen carrier (5) is completely reoxidized, and the air complete reoxidation zone is provided with an air reoxidation tail gas outlet (8). The semi-coke tail gas reduction zone is used to introduce semi-coke tail gas to reduce the oxygen carrier (5). The semi-coke tail gas reduction zone is provided with a reduction tail gas outlet (9). The steam oxidation hydrogen production zone is used to introduce steam to oxidize the reduced oxygen carrier (5) to produce hydrogen. The steam oxidation hydrogen production zone is provided with a first hydrogen outlet (10). One end of the riser (12) is connected to the air complete re-oxidation zone, and the other end is provided with a steam riser chamber (13). The steam riser chamber (13) is connected to the steam oxidation hydrogen production zone through the particle channel (11) set on the third inclined tower plate (4) to form a steam riser secondary oxidation zone. The steam-lift secondary oxidation zone is used to introduce water vapor to supplement the oxidation of the oxygen carrier (5) to produce hydrogen and to fluidize and lift the oxygen carrier (5) to the air complete re-oxidation zone. The steam-lift secondary oxidation zone is provided with a second hydrogen outlet (15).

2. The multi-zone coupled internal circulating fluidized bed reactor according to claim 1, characterized in that, The particle channels (11) are respectively located on the downward tilted side of the first tilted tray (2), the second tilted tray (3) and the third tilted tray (4), and the inlet height of the particle channels (11) is higher than the height of the lowest point of the tilted slope of the oxygen carrier (5) on the corresponding tilted tray.

3. The multi-zone coupled internal circulating fluidized bed reactor according to claim 2, characterized in that, Elbows (17) are provided at the outlets of the particle channels (11) located on the first inclined tray (2) and the second inclined tray (3).

4. The multi-zone coupled internal circulating fluidized bed reactor according to claim 2, characterized in that, The outlet of the particle channel (11) located on the downward side of the third inclined tray (4) is connected to the steam-lifting secondary oxidation zone through the valve port (18).

5. The multi-zone coupled internal circulating fluidized bed reactor according to claim 1, characterized in that, A swirl tube (16) is provided at the connection between the steam-lift secondary oxidation zone and the air complete re-oxidation zone. The second hydrogen outlet (15) is located at the top gas outlet of the swirl tube (16), and the oxygen carrier (5) enters the air complete re-oxidation zone through the bottom of the swirl tube (16).

6. The multi-zone coupled internal circulating fluidized bed reactor according to claim 1, characterized in that, The tilting directions of two adjacent tilted trays are opposite.

7. The multi-zone coupled internal circulating fluidized bed reactor according to claim 1, characterized in that, The main body (1) is a hollow cylindrical structure or a cuboid structure.

8. A hydrogen production system from semi-coke tail gas, characterized in that, It includes an air heater (24), a steam heater (23), a semi-coke tail gas pretreatment device (19), a blower (20), a raw material preheater (21), a raw material gas heater (22) connected in sequence to the semi-coke tail gas outlet, and a multi-zone coupled internal circulation fluidized reactor (26) as described in any one of claims 1-7. The outlet of the raw material gas heater (22) is connected to the high-speed gas inlet (6) and the low-speed gas inlet (7) provided on the second inclined tower plate (3). The air heater (24) is connected to an air source at its inlet and to a gas high-speed inlet (6) and a gas low-speed inlet (7) on the first inclined tower plate (2). The inlet of the steam heater (23) is connected to a steam source, and the outlet of the steam heater (23) is connected to the inlet of the steam lifting chamber (13) and the high-speed gas inlet (6) and low-speed gas inlet (7) on the third inclined tower plate (4).

9. The hydrogen production system from semi-coke tail gas according to claim 8, characterized in that, It also includes a gas cooler (25), the inlet of which is connected to a first hydrogen outlet (10) and a second hydrogen outlet (15), and the outlet of which is connected to a hydrogen storage device.

10. A method for producing hydrogen from semi-coke tail gas using a multi-zone coupled internal circulation fluidized bed reactor as described in any one of claims 1-7, characterized in that, include: After the purified semi-coke tail gas is heated, it is introduced into the semi-coke tail gas reduction zone through the high-speed gas inlet (6) and the low-speed gas inlet (7) on the second inclined tower plate (3), respectively in the form of high-speed semi-coke tail gas and low-speed semi-coke tail gas. The oxygen carrier (5) reacts with the high-speed semi-coke tail gas and is blown up by the high-speed semi-coke tail gas. Part of it falls into the low-speed semi-coke tail gas zone and reacts with the low-speed semi-coke tail gas. Under the action of the second inclined tower plate (3), it is circulated to the high-speed semi-coke tail gas zone. The other part falls into the water vapor oxidation hydrogen production zone along the particle channel (11). The low-speed semi-coke tail gas zone is the area corresponding to the low-speed gas inlet (7) on the second inclined tower plate (3), and the high-speed semi-coke tail gas zone is the area corresponding to the high-speed gas inlet (6) on the second inclined tower plate (3). The reducing tail gas generated after the oxygen carrier (5) reacts with the heated semi-coke tail gas is discharged through the reducing tail gas outlet (9); A portion of the heated steam is introduced into the steam oxidation hydrogen production zone through the high-speed gas inlet (6) and low-speed gas inlet (7) of the third inclined tray (4), respectively, in the form of high-speed steam and low-speed steam; the other portion enters the steam lifting secondary oxidation zone through the steam lifting chamber (13). The oxygen carrier (5) that has reacted with the semi-coke tail gas after falling into the steam oxidation hydrogen production zone reacts with high-speed steam and is blown up by the high-speed steam. Part of it falls into the low-speed steam zone and reacts with the low-speed steam to produce hydrogen, and is circulated to the high-speed steam zone under the action of the third tilted tower plate (4); the other part falls into the steam lifting secondary oxidation zone along the particle channel (11); wherein, the low-speed steam zone is the area corresponding to the low-speed gas inlet (7) on the third tilted tower plate (4), and the high-speed steam zone is the area corresponding to the high-speed gas inlet (6) on the third tilted tower plate (4); The hydrogen produced by the steam oxidation hydrogen production zone is discharged through the first hydrogen outlet (10), and stored after gas-water separation; The oxygen carrier (5) that has fallen into the steam-lifting secondary oxidation zone and reacted with water vapor is lifted along the steam-lifting secondary oxidation zone to the air-complete re-oxidation zone under the action of water vapor introduced into the steam-lifting chamber (13). At the same time, it continues to react with the oxygen carrier (5) that has not completely reacted in the steam-oxidation hydrogen production zone to produce hydrogen. The hydrogen produced by the steam lifting secondary oxidation zone is discharged through the second hydrogen outlet (15), and stored after gas-water separation; The heated air is introduced into the air re-oxidation zone through the high-speed gas inlet (6) and the low-speed gas inlet (7) on the first inclined tower plate (2) in the form of high-speed air and low-speed air, respectively. The oxygen carrier (5) that has been lifted by water vapor to the air re-oxidation zone reacts with high-speed air and is blown up by high-speed air. Part of it falls into the low-speed air zone and reacts with low-speed air, and is circulated to the high-speed air zone under the action of the first tilted tower plate (2); the other part falls into the semi-coke tail gas reduction zone along the particle channel (11) and reacts with semi-coke tail gas, and participates in the next semi-coke tail gas hydrogen production cycle; wherein, the low-speed air zone is the area corresponding to the low-speed gas inlet (7) on the first tilted tower plate (2), and the high-speed air zone is the area corresponding to the high-speed gas inlet (6) on the first tilted tower plate (2); The re-oxidation tail gas generated after the oxygen carrier (5) reacts with heated air is discharged through the air re-oxidation tail gas outlet (8), completing a semi-coke tail gas hydrogen production cycle.

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