Fluidized bed reactor for preparing methanol through continuous CO2 photo-thermal catalytic hydrogenation

Abstract

The invention belongs to the technical field of fluidized bed reactors, and particularly relates to a fluidized bed reactor for preparing methanol through continuous CO2 photo-thermal catalytic hydrogenation. The fluidized bed reactor is composed of five parts including a cone section, a concentrated phase section, a transition section, a dilute phase section and an expansion section from bottom to top in sequence, and the concentrated phase section is provided with a product outlet, an optical assembly and a heat exchange assembly; the diameter of the cross section of the transition section is gradually increased in the direction from the dense-phase section to the dilute-phase section; the expansion section is provided with a cyclone separator, a solid phase outlet at the bottom of the cyclone separator is connected with a return pipe, and the return pipe vertically extends downwards to the concentrated phase section. In conclusion, deep integration of the fluidized bed and photo-thermal catalysis is achieved, the problem of light-mass transfer matching imbalance of a traditional fixed bed is solved, and the light utilization rate and the mass transfer efficiency are improved; an online separation system is integrated, so that continuous production and separation of methanol are realized, and separation energy consumption is reduced; side reaction is inhibited, and catalyst consumption is reduced; a light source is fully utilized, and methanol is prepared through CO2 hydrogenation in a photo-thermal catalysis scene.

Description

Technical Field

[0001] This invention belongs to the field of fluidized bed reactor technology, specifically relating to a continuous CO2 photothermal catalytic hydrogenation fluidized bed reactor for methanol production. Background Technology

[0002] Global CO2 emissions continue to rise, and China has pledged to peak its carbon emissions by 2030 and achieve carbon neutrality by 2060. Therefore, the resource utilization of CO2 (such as conversion to methanol) has become a key technological direction. CO2 conversion technologies mainly include thermochemical conversion, electrochemical reduction, and photocatalytic reduction. Among these, photocatalytic reduction, with its relatively mild reaction conditions, ability to utilize solar energy, high efficiency, and the ability to achieve carbon neutrality throughout its entire life cycle ("green methanol"), is one of the most promising technological pathways.

[0003] Analysis of the reaction equipment used in photocatalytic reduction methods reveals the following main drawbacks: Traditional fixed-bed photocatalytic CO2 reduction reactors suffer from uneven illumination due to catalyst accumulation, low light utilization due to the inability to effectively excite deep-layer catalysts, insufficient contact between reactants and catalysts, poor mass transfer efficiency due to long diffusion paths of intermediates, and the tendency to form local "hot spots," leading to catalyst overheating and deactivation. Existing reactors are mostly batch-type, requiring separate product separation after the reaction, resulting in significant energy losses, inability to achieve continuous production, and difficulty in suppressing side reactions (such as CO and CH4 formation), leading to low methanol selectivity. Reactors used for CO2 hydrogenation to methanol production are primarily designed for thermocatalysis and are not optimized for photocatalysis scenarios. They lack efficient light utilization structures (such as light source dispersion and reflective components), suffer from severe catalyst entrainment, and face difficulties in online product separation, failing to meet the process requirements of CO2 photothermal catalytic methanol production. In summary: ① Imbalance in light-mass transfer, resulting in low light utilization and mass transfer efficiency; ② Low integration, leading to discontinuous methanol production and separation, complex processes, and high energy consumption; ③ Numerous side reactions and high catalyst consumption. Summary of the Invention

[0004] To address the problems existing in the prior art, the present invention provides a continuous CO2 photothermal catalytic hydrogenation fluidized bed reactor for methanol production.

[0005] The technical solution adopted by this invention to solve its technical problem is as follows: A continuous CO2 photothermal catalytic hydrogenation fluidized bed reactor for methanol production, the fluidized bed reactor is composed of five parts, from bottom to top: a conical section, a dense phase section, a transition section, a dilute phase section, and an expansion section; the conical section is provided with a reactant gas inlet, an inert gas inlet, and a gas distribution plate, the gas distribution plate being located inside the upper part of the conical section; the dense phase section is provided with a product outlet, a photoelectric component, and a heat exchange component; the transition section has a cross-sectional diameter that gradually increases from the dense phase section to the dilute phase section; the dilute phase section is provided with a catalyst inlet; the expansion section is equipped with a cyclone separator, the solid phase outlet at the bottom of the cyclone separator being connected to a reflux pipe, the reflux pipe extending vertically downwards to the dense phase section.

[0006] Preferably, in the dense phase segment, the optical component includes: an array lens, which is composed of multiple microlenses arranged in an orderly manner and located on the side of the housing.

[0007] Preferably, the optical component further includes: a sleeve-type first reflector patch and a semi-cylindrical second reflector patch, both of which adopt a patch design. The first reflector patch is arranged longitudinally on the outside of the return pipe at the center of the dense phase section to form a cylindrical reflective layer; the second reflector patch is arranged on the inside of the reactor wall opposite the array lens.

[0008] Preferably, the first reflector patch is a triangular prism structure, and the second reflector patch is a trapezoidal triangular prism.

[0009] Preferably, the first and second reflector patches of the same height are installed at the same height in the dense phase section.

[0010] Preferably, in the dense phase section, the heat exchange assembly includes a heating tube and a condenser tube, both of which are horizontal serpentine structures. The condenser tube is installed on one side of the light source and below the light source inlet, while the heating tube is installed on the opposite side of the light source, and the installation height of the heating tube is higher than that of the condenser tube.

[0011] Preferably, the gas distribution plate adopts a side-slit conical cap type gas distributor.

[0012] Preferably, the dilute phase section is provided with a baffle with small holes.

[0013] Preferably, the bottom end of the return pipe is flared.

[0014] Preferably, a tray is provided at the product outlet.

[0015] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0016] 1. Synergistic optimization of light-mass-heat transfer: The integrated design of fluidized bed and photothermal catalysis in the dense phase section of the reactor. The fluidized bed design suspends and fluidizes the catalyst. By setting up array lenses and two types of reflectors, the structure of light generation and light reflection devices is optimized, the light utilization rate is increased to more than 85%, the gas-solid contact area is increased by 3-5 times, the mass transfer efficiency is improved, and the CO2 conversion rate can reach more than 65%, thus solving the problem of matching light utilization and mass transfer.

[0017] 2. Continuous production and online separation: The reactor integrates "condenser + foldable tray + cyclone separator" to achieve real-time methanol separation, 24-hour continuous production, increased capacity, and reduced methanol liquefaction separation energy consumption by 45% compared with traditional processes.

[0018] 3. Suppression of side reactions and catalyst recycling: The temperature gradient (250℃→150℃) and baffle design in the dilute phase section reduce the side reaction rate to below 5%; the cyclone separator has a separation efficiency of ≥99.5% and the catalyst is recycled with a loss rate of ≤0.5% / day.

[0019] 4. Fluid dynamics optimization: The design of the transition phase diameter in the reactor body, the side slit cone cap of the gas distribution plate, and the baffle design ensure fluidization stability and reduce catalyst entrainment.

[0020] 5. Structural innovation and stability: Foldable trays avoid fluidization interference; horizontal heating / condenser tubes reduce light shading; side-slit conical distributors prevent clogging; reflector patches increase light utilization.

[0021] 6. Material and structure compatibility: 316L stainless steel material and horizontal heating / condenser tubes meet the requirements of high pressure, high temperature, corrosion resistance, and low light shading.

[0022] In summary, this invention achieves deep integration of fluidized bed and photothermal catalysis, solving the problem of "light-mass transfer mismatch" in traditional fixed beds and improving light utilization and mass transfer efficiency; it integrates an online separation system to achieve continuous methanol production and separation, reducing separation energy consumption; it optimizes reactor structure and materials to ensure stable operation at 10MPa and 250℃, suppressing side reactions and reducing catalyst consumption; and it fully utilizes the light source to realize CO2 hydrogenation to methanol in a photothermal catalytic scenario. Attached Figure Description

[0023] Figure 1 This is a schematic diagram of the fluidized bed reactor in this invention.

[0024] Figure 2 yes Figure 1 Cross-sectional view at point AA.

[0025] Figure 3 yes Figure 1 Cross-sectional view at point BB.

[0026] Figure 4 yes Figure 1 Cross-sectional view at CC.

[0027] Figure 5 This is a detailed diagram of the array lens.

[0028] Figure 6 This is a detailed diagram of the first rearview mirror patch.

[0029] Figure 7 This is a detailed diagram of the second rearview mirror patch.

[0030] Figure 8 This is a magnified view of a side-slit conical gas distributor.

[0031] In the picture:

[0032] 1. Conical section, 2. Dense phase section, 3. Transition section, 4. Dilute phase section, 5. Expanding section, 6. Cyclone separator

[0033] 101. Reactant gas inlet; 102. Inert gas inlet; 103. Gas distribution plate.

[0034] 201. Array lens; 202. First reflector patch; 203. Second reflector patch; 204. Heating element; 205. Condenser; 206. Tray; 207. Product outlet; 208. Handle.

[0035] 401. Catalyst inlet; 402. Baffle.

[0036] 601. Return pipe. Detailed Implementation

[0037] To facilitate understanding of the present invention, it will be described in more detail below with reference to the accompanying drawings and specific embodiments. However, the present invention can be implemented in many different forms and is not limited to the embodiments described in this specification. Rather, these embodiments are provided to provide a more thorough and complete understanding of the disclosure of the present invention.

[0038] A continuous CO2 photothermal catalytic hydrogenation fluidized bed reactor for methanol production features a unique layered design and component layout, such as... Figure 1 As shown, the fluidized bed reactor consists of five parts, from bottom to top: conical section 1, dense phase section 2, transition section 3, dilute phase section 4, and expansion section 5. Adjacent structures are fixed together by flange bolts and sealed.

[0039] 1. Conical segment 1

[0040] The bottom of the cone section 1 is provided with an inert gas inlet 102 and the side is provided with a reaction gas inlet 101, which guides the raw material gas (CO2 and H2) into the reactor evenly. The gradual diameter reduces the impact of the airflow. In conjunction with the gas distribution plate 103, the gas forms a uniform airflow, ensuring that the catalyst particles are fluidized smoothly and avoiding local "channeling" or "dead zones".

[0041] Gas distribution plate 103 adopts a side-slit conical cap type gas distributor, combined with Figure 8 understand, Figure 8 Is Figure 1 The image is too small to display and is therefore not labeled. The side-slit conical gas distributor has an opening ratio of 0.01, with the side-slit outlet velocity precisely controlled at 0.026 m / s. This velocity is ≥2 times the horizontal choking velocity of the particles. The unique structure and parameter settings effectively prevent blockage during gas distribution, ensuring the smooth flow of the raw material gas (…). The inert gas, along with the auxiliary fluidizing gas, can be uniformly dispersed into the reactor, laying the foundation for the stable fluidization of the catalyst.

[0042] 2. Dense Phase Section 2 (Main Reaction Zone)

[0043] The core region of the photothermal catalytic reaction is characterized by high catalyst particle concentration and vigorous fluidization, making it ideal for photothermal catalytic reactions. The main reaction zone is equipped with a built-in heating element and light assembly. Catalyst particles are violently fluidized by the airflow, ensuring full contact with the feed gas. Simultaneously, they are excited by the xenon lamp light source (simulating sunlight) to generate electron-hole pairs, efficiently carrying out the reaction of CO2 hydrogenation to methanol. The built-in electric heating assembly maintains a reaction temperature of 250°C, ensuring the reaction rate.

[0044] Structurally, the dense phase section 2 is a cylindrical shell with a product outlet 207 at the bottom. An array lens 201 is innovatively installed on the side of the shell. Figure 5 Understanding this, the lens is composed of multiple microlenses arranged in an orderly manner, which can uniformly disperse the incident xenon lamp light source (whose spectrum is close to sunlight) throughout the entire dense phase section 2, significantly improving the catalyst's light-receiving area and light utilization efficiency. It also includes a sleeve-type first reflector patch 202 and a semi-cylindrical second reflector patch 203, both using a patch design. The first reflector patch 202 has a triangular prism structure, arranged longitudinally on the outer side of the central sleeve of the dense phase section 2, forming a cylindrical reflective layer. The second reflector patch 203 is a trapezoidal triangular prism, arranged on the inner side of the opposite wall of the light source, combined with... Figure 6-7 Understood. The two work together to achieve multiple reflections of light, ensuring that there are no blind spots in the dense phase section 2, allowing the catalyst to be fully excited by light.

[0045] Heating and condensation component design: Combining Figure 2-3The dense phase section 2 contains a horizontal heating tube 204 and a horizontal serpentine condenser tube 205. The heating tube 204 is installed on one side near the second reflector patch 203, and the condenser tube 205 is located on the other side. The installation height of the heating tube 204 is higher than that of the condenser tube 205, and is close to the installation height of the array lens 201. The installation height of the condenser tube 205 is between the array lens 201 and the product outlet 207. The materials, layout, and operating parameters of the heating tube 204 and the condenser tube 205 have all been optimized. The heating tube 204 is made of Inconel 625 alloy, which has excellent high temperature, high pressure, and corrosion resistance. Its horizontal arrangement in the dense phase section 2 reduces light obstruction and can stably maintain the high temperature of 250°C required for the reaction, providing a suitable temperature environment for the photothermal catalytic reaction. The condenser tube 205 is made of 316L stainless steel, and its structural design fully considers the gas-liquid heat exchange requirements. In the dense phase section 2, the condenser tube 205 initially cools the reactant gas from 250℃ to 150℃, preparing for subsequent methanol liquefaction and enabling efficient methanol liquefaction. Throughout the condensation process, the methanol liquefaction rate is ≥98%, and the horizontal layout of the condenser tube 205 effectively reduces obstruction to gas flow.

[0046] In one embodiment, combined Figure 4 It is understood that a foldable tray 206 is provided at the product outlet 207, located below the outlet, for easy product collection. The tray 206 is tightly connected to the reactor wall by a sturdy hinge. In the initial stage of reactor startup, the tray 206 can be completely folded up against the reactor wall without affecting the fluidization state of the catalyst. Once the fluidized bed is running stably, the operator can easily unfold the tray 206 using the external handle 208. After unfolding, the tray 206 can accurately collect the methanol cooled and liquefied by the condenser 205, achieving efficient product collection, and the entire process does not interfere with the gas-solid flow within the reactor.

[0047] 3. Transition Section 3

[0048] Buffered airflow velocity: As the diameter increases, the airflow velocity decreases from 0.01 m / s (operating velocity in the dense phase section) to 0.00345 m / s in the dilute phase section, reducing excessive entrainment of catalyst particles; smoothing the transition flow field avoids turbulent impact caused by abrupt changes in diameter, ensuring reaction continuity.

[0049] 4. Dilute phase section 4

[0050] A catalyst inlet 401 is located near the bottom of the dilute phase section 4, and is positioned close to and inclined towards the transition section 3. The dilute phase section 4 contains perforated baffles 402. Through a rational design of the baffle 402's aperture, number, and arrangement, rising bubbles are effectively separated, enhancing the gas-solid mass transfer process, promoting the continued reaction of incompletely reacted feed gas, and suppressing side reactions. The perforations on the baffle 402 are angled.

[0051] Unreacted feed gas continues to react with the catalyst, prolonging the residence time; lower gas flow rates reduce catalyst agglomeration and suppress side reactions (such as...). To improve methanol selectivity; preliminary cooling: the gas flow temperature is initially reduced from 250°C to 150°C through wall heat exchange (or built-in coil), preparing for subsequent product liquefaction; baffle 402 divides the bubbles, enhances gas-solid mass transfer, and avoids gas short circuit.

[0052] 5. Expanded Section 5

[0053] Further reducing the airflow velocity causes some larger catalyst particles to fall back to the dilute phase section 4 due to gravity, reducing the load on the separator; it also provides a buffer space for gas-solid separation, ensuring a stable flow field at the separator inlet and improving separation efficiency.

[0054] The expanded section 5 is equipped with a cyclone separator 6, which adopts a C-shaped structure design. It utilizes the powerful centrifugal force generated by high-speed rotation to achieve efficient gas-solid separation with a separation efficiency of over 99.5%. The separated catalyst is stably returned to the dense phase section 2 for recycling via the reflux pipe 601.

[0055] 6. Cyclone Separator

[0056] The upper outlet is located at the top of the expansion section 5, and the bottom solid phase outlet is connected to the reflux pipe 601. The reflux pipe 601 extends vertically downward to the dense phase section 2. Its bottom end is lower than the product outlet 207. The bottom end is designed with an flared opening and is located above the gas distribution plate 103.

[0057] Principle: (1) Dust-laden gas enters from the rectangular tangential inlet at the top of the cylinder and flows in a rotating motion along the inner wall of the cylinder; (2) The centrifugal force of the particles is relatively large, so they are thrown to the outer layer, while the airflow is in the inner layer, and the gas and solid are separated. (3) In the conical part, the radius of rotation decreases while the tangential velocity increases, and the airflow and particles move in a downward spiral motion. (4) Near the bottom of the cone, the airflow turns into an upward rotating motion and is finally discharged from the upper outlet pipe; (5) The solid phase falls into the return pipe 601 along the inner wall.

[0058] The catalyst particles entrained in the gas flow are separated by centrifugal force. The separated catalyst is returned to the dense phase section 2 via the reflux pipe 601 for recycling, reducing losses. The purified gas (containing methanol vapor and unreacted gas) enters the subsequent cooling system.

[0059] Working process: The feed gas (a mixture of CO2 and H2 in a 1:3 ratio) enters through the reaction gas inlet 101 on the side of the conical section 1, the catalyst enters through the catalyst feed inlet 401, and simultaneously, inert gas enters through the inert gas inlet 102 at the bottom of the conical section 1, blowing upwards. After being evenly distributed by the gas distribution plate 103, the feed gas fluidizes the Cu / TiO2 catalyst particles in the bed, placing them in a suspended state. During the upward movement, the light source (e.g., an array lens 201 on the side of the dense phase section 2)... Figure 5 As shown, the light is incident into the cavity. The array lens 201 can more evenly disperse the light source into the reactor. A sleeve-shaped first reflector patch 202 is provided at the center of the dense phase section. The first reflector patch 202 is designed in the form of a prism. Figure 6 a) Vertically arranged ( Figure 6 (b) is arranged in a row, with each row attached to the outside of the sleeve to form a sleeve-shaped reflector. Figure 6 c), and a second reflector patch 203 is provided on the vessel wall opposite the incident position of the light source, which can more fully reflect the light source to various positions in the dense phase section 2. It is also a patch design. Considering that the patch is attached to the inner side of the vessel wall to avoid collision between the patches, it is designed as a special prism ( Figure 7 a) The top view is trapezoidal, which avoids collisions when arranged inside the semicircle. Its arrangement is the same as that of reflector patch 1. Figure 6 b), ultimately forming a reflector extending into the interior of half a cylinder ( Figure 7 b). The catalyst is excited by light transmitted through the array lens, while the heating tube 204 provides the thermal conditions, and a photocatalytic hydrogenation reaction occurs in the concentrated phase section 2. The gas-solid mixture after the reaction enters the dilute phase section 4 through the transition section 3 to continue the reaction and suppress side reactions; then it enters the expansion section 5 for deceleration, and the catalyst is separated from the gas by the cyclone separator 6. The catalyst falls back into the bed for recycling; the gaseous methanol is cooled by the condenser 205 to liquefy the methanol and fall onto the tray 206. The tray 206 is connected to the wall of the container by a hinge, so that the tray 206 can be stored when not in use to avoid affecting the fluidization state of the catalyst. After the fluidized bed reaches a stable flow, the tray 206 is opened to collect the product, and finally it is discharged from the product outlet 207.

[0060] Regarding the core reaction parameters and catalyst selection: [The following is a list of parameters and their application] The catalyst possesses a unique microstructure and catalytic performance. Cu nanoparticles are uniformly supported on a TiO2 carrier. The localized surface plasmon resonance effect of Cu significantly enhances visible light absorption while effectively suppressing photogenerated electron-hole recombination, greatly improving the selectivity of CO2 hydrogenation to methanol. Combined with a xenon lamp light source, this source offers stable power, a spectrum close to sunlight (UV-Vis-NIR), fluctuations ≤±2%, and energy consumption more than 30% lower than other light sources, providing precise and efficient excitation energy for the catalyst. The operating pressure is strictly controlled at 10 MPa to ensure good CO2 solubility in the reaction system, thereby increasing the reaction rate; the temperature of the concentrated phase 2 is stably maintained at 250℃. The optimal temperature for catalyst activity is set, and the condensation temperature is set at 65°C to ensure efficient methanol liquefaction and separation.

[0061] Continuous methanol production processes encompass a complete and continuous series of steps, including feed fluidization, photothermal reaction, subsequent reaction cooling, gas-solid separation, and product collection. During the feed fluidization stage, the feed gas ( Inert gas enters precisely from the conical section 1 and is uniformly dispersed by the gas distribution plate 103, causing the Cu / TiO2 catalyst to fluidize and suspend in a suspended state, with the fluidization velocity stabilizing at 0.01 m / s. In the photothermal reaction stage, the xenon lamp light source is uniformly incident on the dense phase section 2 through the array lens 201. Under the 250°C environment maintained by the heating tube 204, the catalyst is photoexcited, undergoing a photocatalytic hydrogenation reaction. In the subsequent cooling stage, the gas-solid mixture enters the dilute phase section 4 via transition section 3. Baffle 402 enhances mass transfer, and the heat exchange tube initially cools the mixture to 150°C, suppressing side reactions. In the gas-solid separation stage, after the mixture enters the expansion section 5 for deceleration, the catalyst is efficiently separated by cyclone separator 6 with a separation efficiency ≥99.5%. The catalyst is returned to the dense phase section 2 for recycling via reflux pipe 601. In the product collection stage, the purified gas containing methanol vapor is cooled to 65°C via condenser 205. The methanol liquefies and falls onto the expanded tray 206, and is continuously discharged from the product outlet 207. Unreacted gas can be recycled back to the reaction gas inlet 101, achieving 24-hour continuous production.

[0062] In this embodiment, a fluidized bed suspends and fluidizes the catalyst. Combined with an array lens and dual-type reflectors, light utilization is increased to over 85%. The gas-solid contact area is increased by 3-5 times, improving mass transfer efficiency, and CO2 conversion rate can reach over 65%, achieving synergistic optimization of light-mass-heat transfer. By integrating a condenser, a foldable tray, and a cyclone separator, methanol liquefaction separation energy consumption is reduced by 45% compared to traditional processes, and 24-hour continuous production is achieved, increasing capacity. The temperature gradient (250℃→150℃) and baffle design in the dilute phase reduce the side reaction rate to below 5%; the cyclone separator has a separation efficiency of ≥99.5%, and the catalyst is recycled, with a loss rate of ≤0.5% / day.

[0063] In one embodiment, the gas distribution plate 103 employs a bubble-type distributor, providing excellent anti-clogging performance. The tray 206 is designed as a drawer-type structure. The light source alternative is a visible light array LED light source. The catalyst alternative can be N-doped catalyst. , Heterojunction catalyst.

[0064] Explanation of relevant professional terms:

[0065] Photothermal catalysis refers to a technology that combines light energy (a specific wavelength light source to excite the catalyst) and heat energy (to maintain the temperature required for the reaction) to achieve a chemical reaction under the action of a catalyst. In this invention, it is used to hydrogenate CO2 and H2 to produce methanol. The core is to generate electron-hole pairs through photoexcitation, while heat energy increases the reaction rate.

[0066] Fluidized bed reactor: A reactor in which solid catalyst particles are suspended and fluidized under the action of fluid (gas), characterized by sufficient gas-solid contact, high mass and heat transfer efficiency, and uniform bed temperature.

[0067] Cyclone separator: A component that uses centrifugal force to achieve gas-solid separation. Gas containing catalyst particles enters and rotates, causing the particles to be thrown against the wall and fall back. The purified gas then enters the subsequent cooling system. In this invention, it is used for catalyst recycling.

[0068] The technical features of the above embodiments can be combined in any way. For the sake of brevity, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

Claims

1. A continuous fluidized bed reactor for the photo-thermal catalytic hydrogenation of CO2 to methanol, characterized in that, The fluidized bed reactor is composed of five parts, from bottom to top, the cone section (1), the dense phase section (2), the transition section (3), the dilute phase section (4) and the expansion section (5); The cone section (1) is provided with a reaction gas inlet (101), an inert gas inlet (102) and a gas distribution plate (103), and the gas distribution plate (103) is located inside the upper part of the cone section (1); The dense phase section (2) is provided with a product outlet (207), a light assembly and a heat exchange assembly; The transition section (3) gradually expands in diameter from the dense phase section (2) to the dilute phase section (4); The dilute phase section (4) is provided with a catalyst inlet (401); The expansion section (5) is equipped with a cyclone separator (6), and the bottom solid phase outlet of the cyclone separator (6) is connected with a reflux pipe (601), which extends vertically downward to the dense phase section (2).

2. The continuous fluidized bed reactor for CO2 photothermocatalytic hydrogenation to methanol according to claim 1, characterized in that, In the dense phase section (2), the light assembly includes an array lens (201) which is composed of a plurality of microlenses arranged in order and located on the side of the shell.

3. The continuous fluidized bed reactor for CO2 photo-thermo catalytic hydrogenation to methanol according to claim 2, characterized in that, The light assembly also includes a sleeve type first mirror patch (202) and a semi-cylindrical second mirror patch (203), both of which are designed as patches, and the first mirror patch (202) is arranged longitudinally outside the reflux pipe (601) in the center of the dense phase section (2), forming a cylindrical light reflecting layer; the second mirror patch (203) is arranged on the opposite side of the reactor wall opposite the array lens (201).

4. The continuous fluidized bed reactor for CO2 photo-thermo catalytic hydrogenation to methanol according to claim 3, characterized in that, The first mirror patch (202) is in the form of a triangular prism, and the second mirror patch (203) is in the form of a trapezoidal triangular prism.

5. The continuous fluidized bed reactor for CO2 photo-thermo catalytic hydrogenation to methanol according to claim 3, characterized in that, The first mirror patch (202) and the second mirror patch (203) are installed at the same height in the dense phase section (2).

6. A continuous fluidized bed reactor for the CO2 photothermal catalytic hydrogenation to methanol according to any one of claims 1 to 5, characterized in that, In the dense phase section (2), the heat exchange assembly includes a heating pipe (204) and a condensing pipe (205), both of which are in the form of horizontal coils, the condensing pipe (205) is installed on the side of the light source below the light source inlet, and the heating pipe (204) is installed on the opposite side of the light source, and the installation height of the heating pipe (204) is higher than that of the condensing pipe (205).

7. The continuous fluidized bed reactor for the CO2-photeiothermal catalytic hydrogenation to methanol according to claim 6, characterized in that The gas distribution plate (103) adopts a side slit cone cap type gas distributor.

8. The continuous fluidized bed reactor for CO2 photo-thermo catalytic hydrogenation to methanol according to claim 6, characterized in that, The dilute phase section (4) is provided with a baffle (402) with small holes.

9. The continuous fluidized bed reactor for CO2 photo-thermo catalytic hydrogenation to methanol according to claim 6, characterized in that, The bottom end of the reflux pipe (601) is designed with a flared end.

10. The continuous fluidized bed reactor for the CO2-photeiothermal catalytic hydrogenation to methanol according to claim 6, characterized in that A tray (206) is provided at the product outlet (207).

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