Reactor for preparing olefin through carbon dioxide hydrogenation

Abstract

The reactor comprises a shell and a dehydration mechanism, a feed gas inlet is formed in the top of the shell, a water outlet is formed in the bottom of the shell, and a product outlet is formed in the lower end of the shell; a partition plate is horizontally and fixedly installed in the shell and located above the product outlet, the space in the shell is divided into an upper cavity and a lower cavity from top to bottom through the partition plate, and a plurality of small holes communicated with the upper cavity and the lower cavity are evenly formed in the partition plate at intervals. The dewatering mechanism is fixedly mounted on the partition plate, the upper end of the dewatering mechanism extends into the upper cavity, and the lower end of the dewatering mechanism extends into the lower cavity and communicates with the water outlet; the upper cavity is filled with a catalyst layer, and the upper portion of the dehydration mechanism extends into the catalyst layer. The device has the beneficial effects that the structure is simple, the design is reasonable, and water generated by reaction can be quickly removed, so that the per-pass conversion rate of CO2 is favorably improved, and the efficient and stable operation of carbon dioxide hydrogenation reaction is ensured.

Description

Technical Field

[0001] The utility model relates to the technical field of catalytic synthesis equipment, in particular to a reactor used for preparing olefins by hydrogenating carbon dioxide. Background Art

[0002] Olefins are an important type of basic industrial raw material, and the global annual olefin consumption shows an increasing trend year by year. Low-carbon olefins mainly refer to ethylene and propylene, which are the basic organic raw materials for synthetic plastics, fibers and other chemical products. High-carbon olefins generally refer to olefins with a carbon number of more than 4. The most widely used are olefins with a carbon number range of C4-C 18 Olefins can be widely used in the production of lubricants, plasticizers and detergents. At present, both low-carbon olefins and high-carbon olefins are mainly produced by petroleum routes. Finding an economical alternative process route to solve the problem of olefin supply and demand caused by rising oil demand has become a problem of great concern to countries around the world.

[0003] CO2 molecules have the characteristics of low adsorption heat and thermodynamic stability, so it is difficult to activate hydrogenation. At present, the research on CO2 hydrogenation to synthesize olefin compounds with high selectivity can be divided into two categories: one is the reaction through oxygen-containing intermediate species such as methanol; the other is through a reaction similar to Fischer-Tropsch synthesis (FTS). Most research works mainly adopt the FTS-like reaction pathway, that is, CO2 first generates CO through the reverse water gas shift (RWGS) reaction, and then CO is hydrogenated to undergo the FTS reaction. Regardless of the pathway, the single-pass yield of carbon dioxide needs to be further improved. Most of the current literature research also focuses on the modification of catalysts to improve the single-pass conversion rate of CO2. There are few studies on the reaction device and reactor for the process of hydrogenation of carbon dioxide to olefins. Since a large amount of water is generated in this process, the chemical reaction equilibrium is broken by continuously removing the water in the product during the reaction, so that the reaction proceeds in the direction of the product, which is conducive to the improvement of the conversion rate.

[0004] Based on this idea, the research and development of a new reactor to continuously remove water from the reaction process to break the conventional chemical reaction balance and improve the single-pass conversion rate of CO2 hydrogenation to produce olefins is an urgent problem to be solved. Utility Model Content

[0005] The utility model provides a reactor for preparing olefins by hydrogenating carbon dioxide, aiming to solve the problems in the prior art.

[0006] The technical solution of the utility model to solve the above technical problems is as follows:

[0007] A reactor for preparing olefins by hydrogenating carbon dioxide comprises a shell and a dehydration mechanism, wherein a raw gas inlet is provided at the top of the shell, a water outlet is provided at the bottom of the shell, and a product outlet is provided at the lower end of the shell; a partition is fixedly installed horizontally in the shell, the partition is located above the product outlet, and the space in the shell is divided into an upper chamber and a lower chamber from top to bottom, and a plurality of small holes connecting the upper chamber and the lower chamber are evenly spaced on the partition; the dehydration mechanism is fixedly installed on the partition, the upper end of the dehydration mechanism extends into the upper chamber, and the lower end of the dehydration mechanism extends into the lower chamber and is connected with the water outlet; the upper chamber is filled with a catalyst layer, and the upper part of the dehydration mechanism extends into the catalyst layer.

[0008] The beneficial effect of the utility model is that in the production process, the raw gas is sent into the shell from the raw gas inlet, and under the catalytic action of the catalyst, the gas generated by the reaction enters the lower cavity through the small holes on the partition and is discharged from the product outlet, and the generated water is discharged from the water outlet through the dehydration mechanism.

[0009] The utility model has a simple structure and a reasonable design, and can quickly remove water generated by the reaction, thereby being beneficial to improving the CO2 single-pass conversion rate and ensuring efficient and stable operation of the carbon dioxide hydrogenation reaction.

[0010] On the basis of the above technical solution, the present invention can also be improved as follows.

[0011] Furthermore, the dehydration mechanism includes at least one dehydration cylinder made of a hydrophilic membrane, each of which is vertically fixed on the partition, with its upper end closed and its lower end open; the upper end of each dehydration cylinder extends into the upper chamber and into the catalyst layer, and the lower end extends into the lower chamber and is connected to the water outlet.

[0012] The beneficial effect of adopting the above further scheme is that in the production process, the raw gas is fed into the shell from the raw gas inlet, and under the catalytic action of the catalyst, the gas produced by the reaction enters the lower chamber through the small holes on the partition and is discharged from the product outlet, and the produced water is discharged from the water outlet through the dehydration cylinder; in addition, the dehydration cylinder made of hydrophilic membrane allows water to pass through, but other products cannot pass through.

[0013] Furthermore, each of the dehydration cylinders further comprises a water-permeable inert carrier, and the hydrophilic membrane is sleeved on the inner surface and / or outer surface of the inert carrier.

[0014] The beneficial effects of adopting the above further scheme are simple structure and reasonable design. The inert carrier can be used as a support to support the hydrophilic membrane, ensuring that the entire dehydration cylinder has a certain strength. In addition, the inert carrier is inactive and avoids affecting the preparation of olefins.

[0015] Furthermore, the dehydration mechanism comprises a plurality of dehydration cylinders, and the plurality of dehydration cylinders are evenly spaced and fixedly mounted side by side on the partition.

[0016] The beneficial effect of adopting the above further scheme is that the number of dehydration cylinders is reasonably designed to ensure the efficiency of olefin production and avoid the produced water affecting the production.

[0017] Furthermore, a joint is fixedly installed at the water outlet, and the lower end of the dehydration cylinder is connected to the upper end of the joint.

[0018] The beneficial effects of adopting the above further solution are simple structure, reasonable design, and connecting the dehydration cylinder and the water outlet through a joint, making drainage more convenient.

[0019] Furthermore, the joint is in a tubular structure with a thick upper end and a thin lower end.

[0020] The beneficial effect of adopting the above further solution is that the shape of the joint is reasonably designed, which is convenient for receiving the water sent by the dehydration cylinder and can quickly discharge the water.

[0021] Furthermore, the upper end of the joint extends into the lower cavity, and the lower end thereof extends outside the shell.

[0022] The beneficial effect of adopting the above further solution is that the two ends of the joint are reasonably distributed.

[0023] Furthermore, it also includes a heat conduction pipe, which is fixedly installed in the catalyst layer and sleeved outside the portion of the dehydration cylinder located in the catalyst layer.

[0024] The beneficial effects of adopting the above further scheme are simple structure, reasonable design, heat transfer to the reaction through the heat pipe, and high reaction efficiency.

[0025] Furthermore, the heat conducting pipe is distributed in the upper cavity in a spiral shape, and both ends of the heat conducting pipe extend to the outside of the shell respectively.

[0026] The beneficial effect of adopting the above further solution is that the heat pipes are reasonably distributed and the heat conduction efficiency is high.

[0027] Furthermore, the shell has a cylindrical structure.

[0028] The beneficial effect of adopting the above further solution is that the overall shape of the shell is neat and beautiful. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 It is a schematic diagram of the overall structure of the utility model;

[0030] Figure 2 It is a structural schematic diagram of the dehydration cylinder in the utility model.

[0031] In the accompanying drawings, the components represented by the reference numerals are listed as follows:

[0032] 1. Shell; 2. Raw gas inlet; 3. Product outlet; 4. Partition; 5. Catalyst layer; 6. Dehydration cylinder; 6-1. Hydrophilic membrane; 6-2. Inert carrier; 7. Joint; 8. Heat pipe. DETAILED DESCRIPTION

[0033] It should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other.

[0034] In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside" and the like indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present utility model. In addition, the terms "first", "second", etc. are only used for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Therefore, features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present utility model, unless otherwise specified, "multiple" means two or more.

[0035] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood by specific circumstances.

[0036] The present invention will be described in detail below with reference to the accompanying drawings and in combination with embodiments.

[0037] Example 1

[0038] like Figure 1 and Figure 2As shown, this embodiment provides a reactor for hydrogenating carbon dioxide to produce olefins, including a shell 1 and a dehydration mechanism, wherein a raw gas inlet 2 is provided at the top of the shell 1, a water outlet is provided at the bottom of the shell 1, and a product outlet 3 is provided at the lower end of the shell 1; a partition 4 is fixedly installed horizontally in the shell 1, and the partition 4 is located above the product outlet 3, which divides the space in the shell 1 from top to bottom into an upper chamber and a lower chamber, and a plurality of small holes connecting the upper chamber and the lower chamber are evenly spaced on the partition 4; the dehydration mechanism is fixedly installed on the partition 4, and its upper end extends into the upper chamber, and its lower end extends into the lower chamber and is connected with the water outlet; the upper chamber is filled with a catalyst layer 5, and the upper part of the dehydration mechanism extends into the catalyst layer 5, and water generated by the reaction of the raw gas in the catalyst layer 5 is discharged from the water outlet through the dehydration mechanism.

[0039] In the production process, the raw gas is fed into the shell 1 from the raw gas inlet 2. Under the catalytic action of the catalyst, the gas produced by the reaction enters the lower chamber through the small holes on the partition 4 and is discharged from the product outlet 3. The produced water is discharged from the water outlet through the dehydration mechanism.

[0040] Preferably, in this embodiment, the partition 4 is preferably a porous plate made of an inert porous material.

[0041] In this embodiment, the porous partition is used to support the catalyst loaded in the reactor. The pore size and number of the porous partition must meet the requirements of: ensuring that the catalyst can be blocked and the reaction gas can flow evenly and smoothly. Therefore, under the premise of meeting the requirements, the more pores the partition has, the larger the pore size, and the more uniform the pore distribution, the more conducive it is to uniform and rapid passage of gas.

[0042] Based on the above scheme, the composition of the above raw gas is: CO2 24vol%, H2 72vol%, 4vol% N2.

[0043] It should be noted that most of the water produced by the reaction of the raw gas entering the shell 1 is discharged from the water outlet after passing through the dehydration mechanism, and a small amount of water and corresponding products enter the lower chamber through several small holes on the partition 4. It is sufficient to ensure that most of the water is removed and that the water that is not removed will not affect the progress of the reaction.

[0044] This embodiment has a simple structure and a reasonable design, and can quickly remove the water generated by the reaction, thereby facilitating the improvement of the CO2 single-pass conversion rate and ensuring the efficient and stable operation of the carbon dioxide hydrogenation reaction.

[0045] Example 2

[0046] On the basis of Example 1, in this embodiment, the dehydration mechanism includes at least one dehydration cylinder 6 made of a hydrophilic membrane 6-1, each of the dehydration cylinder 6 is vertically fixed on the partition 4, with its upper end closed and the lower end open; the upper end of each dehydration cylinder 6 extends into the upper chamber and into the catalyst layer 5, and the lower end extends into the lower chamber and is connected to the water outlet.

[0047] During the production process, the raw gas is fed into the shell 1 through the raw gas inlet 2. Under the catalytic action of the catalyst, the gas produced by the reaction enters the lower chamber through the small holes on the partition 4 and is discharged from the product outlet 3. The produced water is discharged from the water outlet through the dehydration cylinder 6. In addition, the dehydration cylinder 6 made of the hydrophilic membrane 6-1 allows water to pass through, but other products cannot pass through.

[0048] Preferably, in this embodiment, the hydrophilic membrane 6-1 is preferably a PTFE membrane or a molecular sieve membrane in the prior art.

[0049] In addition, the molecular sieve membrane is treated at the acidic site and does not react with the reaction products, and only water can selectively pass through.

[0050] Alternatively, the lower end of each dehydration cylinder 6 is closed and a plurality of through holes are evenly spaced.

[0051] Example 3

[0052] On the basis of Example 2, in this example, each of the dehydration cylinders 6 further includes a water-permeable inert carrier 6 - 2 , and the hydrophilic membrane 6 - 1 is sleeved on the inner surface and / or outer surface of the inert carrier 6 - 2 .

[0053] This solution has a simple structure and a reasonable design. The inert carrier 6-2 can be used as a support to support the hydrophilic membrane 6-1, ensuring that the entire dehydration cylinder 6 has a certain strength. In addition, the inert carrier 6-2 is inactive in nature to avoid affecting the preparation of olefins.

[0054] Preferably, in this embodiment, the above-mentioned inert carrier 6-2 is preferably porous alumina or mullite in the prior art.

[0055] Example 4

[0056] On the basis of any one of Examples 2 to 3, in this example, the dehydration mechanism includes a plurality of dehydration cylinders 6 , and the plurality of dehydration cylinders 6 are evenly spaced and fixedly mounted side by side on the partition 4 .

[0057] The number of dehydration drums 6 is reasonably designed to ensure the efficiency of olefin production and avoid the produced water affecting the production.

[0058] Example 5

[0059] On the basis of any one of Embodiments 2 to 4, in this embodiment, a joint 7 is fixedly installed at the water outlet, and the lower end of the dehydration cylinder 6 is connected to the upper end of the joint 7 .

[0060] This solution has a simple structure and a reasonable design. The dehydration cylinder 6 is connected to the water outlet through the joint 7, so drainage is more convenient.

[0061] Based on the above solution, when there is only one dehydration cylinder 6, the dehydration cylinder 6 and the joint 7 are coaxially arranged.

[0062] When there are multiple dehydration cylinders 6 , the number of dehydration cylinders 6 and the size of the joint 7 are reasonably set to ensure that the lower ends of the multiple dehydration cylinders 6 are connected to the upper ends of the joint 7 respectively.

[0063] Example 6

[0064] On the basis of Example 5, in this embodiment, the joint 7 is in a tubular structure with a thick upper end and a thin lower end.

[0065] The shape of the joint 7 is reasonably designed, which is convenient for receiving the water sent by the dehydration cylinder 6 and can quickly discharge the water.

[0066] Alternatively, the joint 7 may be a joint with the same size at both ends.

[0067] Example 7

[0068] On the basis of any one of Embodiments 5 to 6, in this embodiment, the upper end of the connector 7 extends into the lower cavity, and the lower end thereof extends outside the shell 1 .

[0069] The two ends of the joint 7 are reasonably distributed.

[0070] Example 8

[0071] On the basis of the above embodiments, this embodiment further includes a heat conducting pipe 8 , which is fixedly installed in the catalyst layer 5 and sleeved outside the portion of the dehydration cylinder 6 located in the catalyst layer 5 .

[0072] This solution has a simple structure and a reasonable design. Heat is transferred to the reaction through the heat pipe 8, and the reaction efficiency is high.

[0073] Based on the above solution, the heat pipes 8 are distributed in the catalyst layer 5 .

[0074] The heat pipe 8 is used to quickly remove the reaction heat. The heat pipe 8 is installed on the catalyst bed, and according to the different heat release of the catalyst bed reaction, the heat pipe 8 with different thermal conductivity can be selected.

[0075] Example 9

[0076] On the basis of Example 8, in this embodiment, the heat pipe 8 is distributed in the upper cavity in a spiral shape, and both ends thereof extend to the outside of the shell 1 respectively.

[0077] The heat conducting pipes 8 are reasonably distributed and have high heat conducting efficiency.

[0078] Preferably, in this embodiment, heat transfer oil flows in the heat transfer pipe 8 .

[0079] Alternatively, the portion of the heat conducting pipe 8 located in the upper cavity is vertically distributed and wavy.

[0080] Example 10

[0081] On the basis of the above embodiments, in this embodiment, the shell 1 is a cylindrical structure.

[0082] The overall shape of the housing 1 is neat and beautiful.

[0083] Based on the above solution, each of the above dehydration cylinders 6 is preferably a cylindrical structure.

[0084] In addition, the partition plate 4 is preferably a circular plate-shaped structure, and the joint 7 is preferably a cylindrical structure.

[0085] The working principle of the utility model is as follows:

[0086] CO2 hydrogenation to olefins reaction: The catalyst in the reactor is diluted and filled with porcelain balls (the dilution ratio of iron-based catalyst to porcelain balls is 1:4), the iron-based catalyst is KFe100Al30, the dosage is 10g, and a dehydration device is used. In this system, the raw gas (CO224vol%, H2 72vol%, 4vol%N2) enters the catalyst reaction bed through the raw gas inlet pipe, the gas containing olefin products after the reaction flows out of the reactor through the reactor outlet, and the water generated during the reaction penetrates through the dehydration device and is discharged from the water outlet. When the reaction is running, the heat exchange system of the reaction device is started at the same time (the heat transfer pipe uses heat transfer oil, the heat transfer oil enters the heat transfer pipe through the heat transfer pipe inlet, and flows out from the heat transfer pipe outlet of the reaction to the heat transfer oil heat exchange equipment through the heat transfer pipeline in the reactor).

[0087] The specific steps of the carbon dioxide hydrogenation reaction to produce olefins are as follows:

[0088] Step (1) The catalyst is subjected to reduction pretreatment; the pretreated gas (CO2 24 vol%, H2 72 vol%, 4 vol% N2) entering the reactor passes through the catalyst bed and is subjected to atmospheric pressure reduction pretreatment, and is reduced at 350°C for 8 hours.

[0089] In step (2), the raw gas is preheated to a temperature of 280° C. and enters the reactor through the raw gas inlet pipe for a high-pressure catalytic reaction.

[0090] Step (3) The high-temperature and high-pressure reaction gas entering the reactor reacts in the reactor designed in the utility model to obtain a reaction mixture. The reaction temperature is 320°C, the pressure is 1.5 MPa, and the space velocity is 5000 mL·g catalyst. -1 ·h -1 .

[0091] In the utility model, the reactor is combined with the characteristics of the catalyst, and the catalyst needs to be diluted and filled with inert materials. This type of filling method of the reactor, combined with the heat pipe, ensures the uniform distribution of reaction heat and the timely removal of excessive reaction heat when the reactor is reacting, thereby ensuring the uniform distribution of the temperature of the catalyst bed, ensuring the stable reaction performance of the catalyst and the safe operation of the reactor.

[0092] In view of the technical problems in the process of catalyzing CO2 hydrogenation to olefins by current catalysts, that is, a large amount of water is generated in the reaction, resulting in a large amount of water in the product, and the conversion rate of CO2 hydrogenation to olefins is also low, in order to solve the above problems, the utility model provides a new reactor. The reactor has a cylindrical tubular shell, which provides sufficient space for rapid reaction; a porous partition supporting iron catalyst material, and a diluted iron catalyst is filled above the partition; a heat dissipation pipe dispersed between the porous partitions is used to regulate and remove the heat generated during the catalytic reaction; and a dehydration mechanism is provided to quickly remove the water generated by the reaction, thereby facilitating the improvement of the CO2 single-pass conversion rate.

[0093] The reactor is suitable for the characteristics of the catalytic CO2 hydrogenation to olefins reaction process. The reactor designed by the utility model has the advantages of high CO2 single-pass conversion rate and continuous and stable operation.

[0094] The beneficial effects that the utility model can produce are as follows:

[0095] 1) The dehydration mechanism provided by the utility model can continuously remove the water generated in the reaction process, so that the carbon dioxide hydrogenation reaction is more conducive to the direction of the product olefins, thereby improving the single-pass conversion rate of carbon dioxide. In addition, the dehydration mechanism can better separate the olefin product and water during the reaction process, which is beneficial to the separation of later products.

[0096] 2) The reactor and heat conduction device provided by the utility model make the reactor of the utility model more stable in operation than the traditional fixed bed reactor, the catalyst bed temperature is evenly distributed, and the operating temperature is easy to control, ensuring that the reaction heat is not only evenly distributed in the catalyst bed, but also can be evenly removed, ensuring the stable progress of the reaction, safety and efficiency.

[0097] Table 1 shows the conversion of reactant CO2 and total olefin selectivity during the nearly 1000 hours of reaction time.

[0098] Table 1

[0099] Running time (h) <![CDATA[Conversion rate of CO2 (mol%)]]> Total olefins / total hydrocarbons (mol%) 10 42.4 75.6 200 41.5 78.8 400 40.1 78.4 600 40.7 78.7 800 40.5 77.5 1000 40.4 76.9

[0100] The reaction results show that in this reactor, during the nearly 1000 hours of operation, the conversion rate of the reactant CO2 and the total olefin selectivity remained basically stable, the catalyst bed temperature was evenly distributed (310-340°C), and no obvious hot spots appeared.

[0101] Comparative Example

[0102] It only uses a traditional fixed bed reactor with heat transfer oil and does not contain a dehydration device.

[0103] Table 2

[0104] Running time (h) <![CDATA[Conversion rate of CO2 (mol%)]]> Total olefins / total hydrocarbons (mol%) 10 32.3 75.1 200 31.9 78.1 400 30.1 78.6 600 30.6 78.8 800 30.9 77.3 1000 30.4 76.6

[0105] It can be seen from the above content that in this reactor, the carbon dioxide conversion rate in the conventional technology is significantly lower than that of the reactor using the dehydration mechanism in the utility model.

[0106] It is obvious to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or essential features of the present invention. Therefore, the embodiments should be regarded as exemplary and non-restrictive from any point of view, and the scope of the present invention is defined by the appended claims rather than the above description, and it is intended that all changes falling within the meaning and scope of the equivalent elements of the claims be included in the present invention. Any reference numeral in a claim should not be regarded as limiting the claim to which it relates.

[0107] In addition, it should be understood that although the present specification is described according to implementation modes, not every implementation mode contains only one independent technical solution. This description of the specification is only for the sake of clarity. Those skilled in the art should regard the specification as a whole. The technical solutions in each embodiment may also be appropriately combined to form other implementation modes that can be understood by those skilled in the art.

[0108] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principles of the present invention should be included in the protection scope of the present invention.

Claims

1. A reactor for producing olefins by hydrogenating carbon dioxide, characterized in that: The invention comprises a shell (1) and a dehydration mechanism, wherein a raw gas inlet (2) is provided at the top of the shell (1), a water outlet is provided at the bottom of the shell (1), and a product outlet (3) is provided at the lower end of the shell (1); a partition (4) is fixedly installed horizontally in the shell (1), the partition (4) is located above the product outlet (3), and divides the space in the shell (1) from top to bottom into an upper chamber and a lower chamber, and a plurality of small holes connecting the upper chamber and the lower chamber are evenly spaced on the partition (4); the dehydration mechanism is fixedly installed on the partition (4), the upper end of which extends into the upper chamber, and the lower end of which extends into the lower chamber and is connected to the water outlet; the upper chamber is filled with a catalyst layer (5), and the upper part of the dehydration mechanism extends into the catalyst layer (5).

2. The reactor for preparing olefins by hydrogenation of carbon dioxide according to claim 1, characterized in that: The dehydration mechanism comprises at least one dehydration cylinder (6) made of a hydrophilic membrane (6-1), each of the dehydration cylinders (6) being vertically fixedly mounted on the partition (4), with its upper end being closed and its lower end being open; the upper end of each of the dehydration cylinders (6) extending into the upper chamber and into the catalyst layer (5), and the lower end extending into the lower chamber and communicating with the water outlet.

3. The reactor for preparing olefins by hydrogenation of carbon dioxide according to claim 2, characterized in that: Each of the dehydration cylinders (6) further comprises a water-permeable inert carrier (6-2), and the hydrophilic membrane (6-1) is sleeved on the inner surface and / or outer surface of the inert carrier (6-2).

4. The reactor for preparing olefins by hydrogenation of carbon dioxide according to claim 2, characterized in that: The dehydration mechanism comprises a plurality of dehydration cylinders (6), and the plurality of dehydration cylinders (6) are evenly spaced and fixedly mounted side by side on the partition plate (4).

5. The reactor for preparing olefins by hydrogenating carbon dioxide according to any one of claims 2 to 4, characterized in that: A joint (7) is fixedly installed at the water outlet, and the lower end of the dehydration cylinder (6) is connected to the upper end of the joint (7).

6. The reactor for preparing olefins by hydrogenating carbon dioxide according to claim 5, characterized in that: The joint (7) is in a tubular structure with a thick upper end and a thin lower end.

7. The reactor for preparing olefins by hydrogenating carbon dioxide according to claim 5, characterized in that: The upper end of the joint (7) extends into the lower cavity, and the lower end of the joint extends outside the shell (1).

8. The reactor for preparing olefins by hydrogenating carbon dioxide according to any one of claims 2 to 4, characterized in that: It also comprises a heat conducting pipe (8), which is fixedly installed in the catalyst layer (5) and sleeved outside the portion of the dehydration cylinder (6) located in the catalyst layer (5).

9. The reactor for preparing olefins by hydrogenating carbon dioxide according to claim 8, characterized in that: The heat conducting pipe (8) is distributed in the upper cavity in a spiral shape, and both ends thereof extend to the outside of the shell (1) respectively.

10. The reactor for preparing olefins by hydrogenating carbon dioxide according to any one of claims 1 to 4, characterized in that: The shell (1) is in a cylindrical structure.

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