Reaction system for removing oxides in Fischer-Tropsch synthetic oil

Abstract

The invention provides a reaction system for removing oxides in Fischer-Tropsch synthetic oil, the reaction system comprises a segmented reactor, a tube nest and a baffle plate, the segmented reactor is provided with a feed gas distribution cavity, a plurality of heating cavities and a product cavity which are sequentially spaced, each heating cavity is provided with a heat exchange medium inlet and a heat exchange medium outlet, the extension direction of the array tubes is parallel to the extension direction of the segmented reactor, the array tubes are distributed in the segmented reactor at intervals, openings in the two ends of any array tube respectively extend to the feed gas distribution cavity and the product cavity, and the array tubes are filled with a metal oxide catalyst; a plurality of baffle plates inclined relative to the horizontal plane are arranged in any heating cavity, the heat exchange medium inlet is located above the uppermost baffle plate, and the multiple baffle plates are used for conducting bending and flow guiding on a heat medium so that the heat medium can flow through different positions of the multiple tube nests in the axial direction in the falling process. According to the technical scheme provided by the invention, the performance of the reaction system for removing the oxides in the Fischer-Tropsch synthetic oil can be improved.

Description

Technical Field

[0001] The invention relates to the technical field of Fischer-Tropsch synthetic oil, and in particular to a reaction system for removing oxides in Fischer-Tropsch synthetic oil. Background Art

[0002] The removal of oxides from Fischer-Tropsch synthetic oil is a reaction system with high requirements for heat exchange. For this reaction system, if a single-tube reactor is used, the isomerization of α-olefins will occur due to the long pipeline; if a fixed-bed reactor is used, the removal rate of oxides will be affected due to the uneven temperature distribution of the bed layer; the traditional shell-and-tube fixed-bed reactor has a large heat exchange area per unit volume of catalyst, but the single arched baffle or circular-annular baffle installed at 90° generally has a dead zone in a certain range during the fluid flow process. The heat exchange effect of the reaction tube at this position may be affected, resulting in problems such as sintering of the catalyst in the tube, temperature runaway, or an increase in reaction by-products. Summary of the invention

[0003] The invention provides a reaction system for removing oxides in Fischer-Tropsch synthetic oil, so as to improve the performance of the reaction system for removing oxides in Fischer-Tropsch synthetic oil.

[0004] In order to achieve the above-mentioned purpose, the present invention provides a reaction system for removing oxides from Fischer-Tropsch synthetic oil. The reaction system for removing oxides from Fischer-Tropsch synthetic oil comprises a segmented reactor, a tube array and a baffle. The segmented reactor comprises a raw gas distribution chamber, a plurality of heating chambers and a product chamber which are sequentially spaced from top to bottom. Any heating chamber has a heat exchange medium inlet and a heat exchange medium outlet. The Fischer-Tropsch synthetic oil raw gas to be free of oxides enters from the raw gas distribution chamber and is finally discharged from the product chamber. The extension direction of the tube array is parallel to the extension direction of the segmented reactor. There are a plurality of tube arrays which are spaced at intervals in the segmented reactor. The openings at both ends of any tube array extend to the raw gas distribution chamber and the product chamber respectively. The tube array is filled with a metal oxide catalyst. A plurality of baffles inclined relative to a horizontal plane are arranged in any heating chamber. The heat exchange medium inlet is located above the uppermost baffle. The plurality of baffles are used to bend and guide the heat medium so that the heat medium flows through different axial positions of the plurality of tube arrays during the falling process.

[0005] Further, in the radial direction of the segmented reactor, one side of the baffle is fixedly connected to the inner wall of the segmented reactor, and the other side of the baffle at least extends downwardly in an inclined manner to the center line of the segmented reactor.

[0006] Furthermore, for any heating chamber, the multiple baffles inside it are spaced apart along the axial direction of the segmented reactor, and any two adjacent baffles are staggered in the circumferential direction of the segmented reactor, and the projections of the two on the radial plane of the segmented reactor on the side close to the center line of the segmented reactor at least partially overlap.

[0007] Furthermore, for any heating chamber, the projection centers of any two adjacent baffles inside the chamber on the radial plane of the segmented reactor are symmetrically arranged and cover the projection of the heating chamber on the radial plane of the segmented reactor.

[0008] Furthermore, for any heating chamber, the inclination angles of the multiple baffles inside the chamber are the same.

[0009] Furthermore, the inclination angle of the baffle is α=30°~45°.

[0010] Furthermore, the metal oxide catalyst is one or more of Al2O3, SiO2, TiO2, ZnO, Ga2O3, and MgO modified by one or more of Cu, Ni, Zn, Mg, Ca, and Co.

[0011] Furthermore, the segmented reactor includes an upper head, a shell and a lower head connected in sequence from top to bottom, the cavity in the upper head forms a raw gas distribution chamber, the cavity in the lower head forms a product chamber, a plurality of partitions are arranged in the shell along its axial direction, the raw gas distribution chamber and the adjacent heating chamber are separated by a partition, the product chamber and the adjacent heating chamber are separated by a partition, and the remaining partitions are used to divide the shell into multiple heating chambers, and the openings at both ends of the tube array extend to the two partitions located at the two ends respectively.

[0012] Furthermore, the reaction system for removing oxides from Fischer-Tropsch synthetic oil also includes a distributor arranged in the upper head, and the distributor is externally connected to a feeding device to evenly distribute the gaseous raw materials transported to the upper head by the feeding device in the raw gas distribution chamber.

[0013] Furthermore, the reaction system for removing oxides from Fischer-Tropsch synthetic oil also includes a raw material preheater and a product heat exchanger. The raw material preheater is arranged on an external pipeline between the feeding equipment and the distributor to heat the raw material transported by the feeding equipment to make it gaseous. The product heat exchanger is arranged on an external pipeline connected to the bottom of the lower head to cool the discharged material.

[0014] By applying the technical solution of the present invention, a reaction system for removing oxides from Fischer-Tropsch synthetic oil is provided. The reaction system for removing oxides from Fischer-Tropsch synthetic oil comprises a segmented reactor, tubes and baffles. The segmented reactor comprises a raw gas distribution chamber, a plurality of heating chambers and a product chamber which are sequentially spaced from top to bottom. Any heating chamber has a heat exchange medium inlet and a heat exchange medium outlet. The Fischer-Tropsch synthetic oil raw gas to be free of oxides enters from the raw gas distribution chamber and is finally discharged from the product chamber. The extension direction of the tubes is parallel to the extension direction of the segmented reactor. There are a plurality of tubes which are spaced at intervals in the segmented reactor. Openings at both ends of any tube extend to the raw gas distribution chamber and the product chamber respectively. The tubes are filled with metal oxide catalysts. A plurality of baffles inclined relative to a horizontal plane are arranged in any heating chamber. The heat exchange medium inlet is located above the uppermost baffle. The plurality of baffles are used to bend and guide the heat medium so that the heat medium flows through different axial positions of the plurality of tubes during the falling process.

[0015] This solution is adopted to achieve heating of different regions in the length direction of the tube array by setting a plurality of heating chambers connected in sequence, so as to ensure the consistency and stability of heating of the parts of the tube array located in different heating chambers as needed, thereby ensuring the consistency of the reaction degree in the tube array in each heating chamber, which is beneficial to improving the reaction efficiency. On the other hand, by setting a baffle to block the flow direction of the heat exchange medium in the heating chamber, the heat exchange medium can be evenly heated to different positions in the length direction of the tube array in the form of baffles, avoiding the situation where the reaction efficiency and effect of the Fischer-Tropsch synthesis oil raw material gas (i.e., gas phase raw material) and the metal oxide catalyst inside the tube array are affected by uneven heating of the tube array, which is beneficial to improving the removal efficiency and effect of the oxide without increasing the isomerization rate of α-olefins. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] The drawings constituting a part of the present application are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the drawings:

[0017] Figure 1 A schematic structural diagram of a reaction system for removing oxides from Fischer-Tropsch synthetic oil provided by an embodiment of the present invention is shown.

[0018] The above drawings include the following reference numerals:

[0019] 10. Segmented reactor; 101. Raw gas distribution chamber; 102. Heating chamber; 103. Product chamber; 104. Heat exchange medium inlet; 105. Heat exchange medium outlet;

[0020] 11. Upper head; 12. Shell; 13. Lower head; 14. Partition;

[0021] 20. Listing;

[0022] 30. Baffle;

[0023] 41. Distributor; 42. Preheater; 43. Product heat exchanger. DETAILED DESCRIPTION

[0024] The technical solutions in the embodiments of the present invention will be described clearly and completely below in conjunction with the accompanying drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all of the embodiments. The following description of at least one exemplary embodiment is actually only illustrative and is by no means intended to limit the present invention and its application or use. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0025] like Figure 1 As shown, an embodiment of the present invention provides a reaction system for removing oxides from Fischer-Tropsch synthesis oil, and the reaction system for removing oxides from Fischer-Tropsch synthesis oil comprises a segmented reactor 10, a tube array 20 and a baffle 30, the segmented reactor 10 has a raw gas distribution chamber 101, a plurality of heating chambers 102 and a product chamber 103 sequentially spaced from top to bottom, any heating chamber 102 has a heat exchange medium inlet 104 and a heat exchange medium outlet 105, the Fischer-Tropsch synthesis oil raw gas to be deoxidized enters from the raw gas distribution chamber 101 and is finally discharged from the product chamber 103; the tube array 20 The extension direction is parallel to the extension direction of the segmented reactor 10. There are multiple tube arrays 20 and they are distributed at intervals in the segmented reactor 10. The openings at both ends of any tube array 20 extend to the feed gas distribution chamber 101 and the product chamber 103 respectively. The tube arrays 20 are filled with metal oxide catalysts. Any heating chamber 102 is provided with multiple baffles 30 inclined relative to the horizontal plane. The heat exchange medium inlet 104 is located above the uppermost baffle 30. The multiple baffles 30 are used to bend and guide the heat medium so that the heat medium flows through different axial positions of the multiple tube arrays 20 during the falling process.

[0026] In this embodiment, heating of different regions in the length direction of the tube array 20 is achieved by setting a plurality of sequentially connected heating chambers 102, so as to ensure the consistency and stability of heating of the parts of the tube array 20 located in different heating chambers 102 as needed, thereby ensuring the consistency of the reaction degree in the tube array 20 in each heating chamber 102, which is beneficial to improving the reaction efficiency. On the other hand, the flow direction of the heat exchange medium in the heating chamber 102 is baffled by setting a baffle plate 30, so that the heat exchange medium can be evenly heated to different positions in the length direction of the tube array 20 in the form of baffles, avoiding the situation where the reaction efficiency and effect of the Fischer-Tropsch synthesis oil feedstock gas (i.e., gas-phase feedstock) and the metal oxide catalyst inside the tube array 20 are affected by uneven heating of the tube array 20, which is beneficial to improving the removal efficiency and effect of the oxide without increasing the isomerization rate of α-olefins.

[0027] Preferably, the temperature of the heat exchange medium flowing through the multiple different heating chambers 102 is the same, or the temperature difference of the heat exchange medium flowing through any two different heating chambers 102 does not exceed 0.5°C, ensuring that the temperature of each heating chamber 102 is the same or similar, and the consistency of heating of the parts of the tube array 20 located in different heating chambers 102 is ensured by limiting the temperature. On the other hand, the multiple tube arrays 20 in this embodiment are regularly arranged in the segmented reactor 10, so that Figure 1 For example, it includes at least 3 tubes 20, wherein the axis of one tube 20 coincides with the center line of the segmented reactor 10, and the other two tubes 20 are symmetrically distributed on both sides of the middle tube 20, or in other embodiments not shown in the figure, the tube 20 whose axis coincides with the center line of the segmented reactor 10 is not included, and multiple tubes 20 are equidistantly distributed around the center line. It can be understood that the number and distribution of the tubes 20 can be adjusted according to actual conditions, and the temperature of the heat exchange medium flowing through multiple different heating chambers 102 can also be adaptively adjusted according to actual conditions, and is not limited to the above embodiments.

[0028] Specifically, the heat exchange medium outlet 105 and the heat exchange medium inlet 104 are respectively arranged at the bottom and the top of the opposite sides of the heating chamber 102. It can be understood that the heat exchange medium outlet 105 and the heat exchange medium inlet 104 can be opened and closed.

[0029] like Figure 1 As shown, in the radial direction of the segmented reactor 10 , one side of the baffle plate 30 is fixedly connected to the inner wall of the segmented reactor 10 , and the other side of the baffle plate 30 at least extends downwardly inclined to the center line of the segmented reactor 10 .

[0030] This embodiment, by limiting the extension position of the side of the baffle 30 not connected to the segmented reactor 10, is conducive to ensuring that the heat exchange medium after being guided by the baffle 30 can at least pass through the multiple tubes 20 on one side of the center line, thereby ensuring the reliability of heating at different positions in the length direction of the tubes 20. On the other hand, by limiting the downward inclination of the baffle 30, it is conducive to receiving and guiding the heat exchange medium falling from the heat exchange medium inlet 104, which improves the guiding effect of the heat exchange medium compared to the case of placing the baffle 30 horizontally, and also avoids the accumulation of the heat exchange medium on the baffle 30.

[0031] Optionally, the heat exchange medium may be high temperature steam or heat transfer oil.

[0032] Specifically, for any heating chamber 102, the multiple baffles 30 inside it are spaced apart along the axial direction of the segmented reactor 10, and any two adjacent baffles 30 are staggered in the circumferential direction of the segmented reactor 10, and the projections of the two sides close to the center line of the segmented reactor 10 on the radial plane of the segmented reactor 10 at least partially overlap. This arrangement ensures that the baffle 30 located at the bottom can receive the heat exchange medium under the guidance of the baffle 30 above, ensuring the bending and guiding effect on the heat exchange medium.

[0033] Furthermore, for any heating chamber 102 , any two adjacent baffles 30 inside the heating chamber 102 are symmetrically arranged in the projection center on the radial plane of the segmented reactor 10 and cover the projection of the heating chamber 102 on the radial plane of the segmented reactor 10 .

[0034] This arrangement ensures the reliability of the next baffle 30 in receiving and guiding the heat exchange medium guided by the previous baffle 30, avoids the situation where part of the heat exchange medium directly crosses the next baffle 30 and falls directly, and ensures the bending and guiding effect.

[0035] Among them, for any heating chamber 102, the inclination angles of the multiple baffles 30 inside it are the same. Such a setting is conducive to improving the baffle effect and the stability of the baffle, and avoiding the situation where the angle difference between two adjacent baffles 30 is large, resulting in poor or unstable guiding effect.

[0036] Preferably, the inclination angles of the multiple baffles 30 in each heating chamber 102 are the same.

[0037] Furthermore, the inclination angle α of the baffle 30 is 30° to 45°. This arrangement avoids the situation where the inclination angle of the baffle 30 is too small and the flow guiding effect is poor, and when the inclination angle of the baffle 30 is too small or too large, the guided fluid will be too concentrated in the middle area near the segmented reactor 10, and the heat conduction effect on the tubes 20 located in the two side areas is poor. This is conducive to improving the flow guiding effect and ensuring uniform heating of the tubes 20 at different heights in the heating chamber 102.

[0038] Preferably, the metal oxide catalyst is one or more of Al2O3, SiO2, TiO2, ZnO, Ga2O3, MgO modified by one or more of Cu, Ni, Zn, Mg, Ca, Co. Among them, the Al2O3, SiO2, TiO2, ZnO, Ga2O3, MgO carriers are prepared by hydrothermal reaction at 180-300°C with Al(OH)3, silicate, TiCl4, Zn(OH)2, Ga(NO3)3, M(OH)2 as precursors, and then Cu, Ni, Zn, Mg, Ca, Co, Sr metals are loaded onto the carrier surface by photocatalysis, and the metal loading amount is 1wt%-20wt%, preferably 3wt%-8wt%.

[0039] like Figure 1 As shown, the segmented reactor 10 includes an upper head 11, a shell 12 and a lower head 13 connected in sequence from top to bottom, the cavity in the upper head 11 forms a raw gas distribution chamber 101, the cavity in the lower head 13 forms a product chamber 103, a plurality of partitions 14 are arranged in the shell 12 along its axial direction, the raw gas distribution chamber 101 and the adjacent heating chamber 102 are separated by a partition 14, the product chamber 103 and the adjacent heating chamber 102 are separated by a partition 14, and the remaining partitions 14 are used to divide the shell 12 into a plurality of heating chambers 102, and the openings at both ends of the array tube 20 extend to the two partitions 14 located at the two ends respectively. This arrangement facilitates the separation and forming of the raw gas distribution chamber 101, the plurality of heating chambers 102 and the product chamber 103.

[0040] Specifically, in this embodiment, one end opening of the tube array 20 is formed on the partition 14 between the raw gas distribution chamber 101 and the adjacent heating chamber 102, and the other end opening of the tube array 20 is formed on the partition 14 between the product chamber 103 and the adjacent heating chamber 102, so as to ensure the reliability of gas distribution and avoid the situation where the opening of the tube array 20 extends too deeply into the raw gas distribution chamber 101, resulting in the Fischer-Tropsch synthetic oil raw gas (i.e., gas-phase raw material) being easily accumulated at the bottom of the raw gas distribution chamber 101. At the same time, it avoids the situation where the other opening of the tube array 20 extends too deeply into the product chamber 103, resulting in the accumulation of product materials at the same position, which is not conducive to discharge.

[0041] Preferably, the array of tubes 20 can be switched on and off at the two partitions of any heating chamber 102. Specifically, after the deoxygenation reaction of the Fischer-Tropsch synthesis oil raw gas (i.e., gas-phase raw material) in the array of tubes 20 in the previous heating chamber 102 is completed, the Fischer-Tropsch synthesis oil raw gas (i.e., gas-phase raw material) can continue to enter the array of tubes 20 in the next heating chamber 102 for the next reaction. This arrangement is conducive to increasing the reaction time and reaction effect of the Fischer-Tropsch synthesis oil raw gas (i.e., gas-phase raw material) in each heating chamber 102, thereby improving the oxide removal effect of the reaction system for removing oxides in the Fischer-Tropsch synthesis oil on the Fischer-Tropsch synthesis oil raw gas (i.e., gas-phase raw material).

[0042] like Figure 1 As shown, the reaction system for removing oxides from Fischer-Tropsch synthesis oil also includes a distributor 41 disposed in the upper end cap 11, and the distributor 41 is externally connected to a feeding device to uniformly distribute the gaseous raw materials transported by the feeding device to the upper end cap 11 in the raw gas distribution chamber 101. This arrangement is conducive to the uniform distribution of the Fischer-Tropsch synthesis oil raw gas (i.e., gaseous raw material) in the raw gas distribution chamber 101, thereby ensuring the uniformity and reliability of the distribution of the Fischer-Tropsch synthesis oil raw gas (i.e., gaseous raw material) into the multiple tube arrays 20.

[0043] Specifically, the reaction system for removing oxides from the Fischer-Tropsch synthesis oil also includes a raw material preheater 42 and a product heat exchanger 43. The raw material preheater 42 is arranged on the external pipeline between the feeding device and the distributor 41 to heat the raw material transported by the feeding device to make it gaseous, and the product heat exchanger 43 is arranged on the external pipeline connected to the bottom of the lower head 13 to cool the discharged material. In this arrangement, the Fischer-Tropsch synthesis oil is preheated into the Fischer-Tropsch synthesis oil raw material gas (i.e., gaseous raw material) by the raw material preheater 42, which is conducive to the input of the Fischer-Tropsch synthesis oil and the removal of oxides; the cooling of the material from which the oxides have been removed is achieved by the product heat exchanger 43.

[0044] In summary, the present invention provides a reaction system for removing oxides from Fischer-Tropsch synthetic oil, and its working principle includes: the raw material preheater 42 heats the Fischer-Tropsch synthetic oil raw material to a certain temperature according to the different Fischer-Tropsch synthetic oil raw materials added, and enters the segmented reactor 10 in a gas phase (i.e., Fischer-Tropsch synthetic oil raw gas), and the Fischer-Tropsch synthetic oil raw gas is evenly dispersed through the distributor 41 and enters the multiple tubes 20 loaded with catalyst. The heat exchange medium that provides heat to each heating chamber 102 enters the heating chamber 102 through the heat exchange medium inlet 104, and in order to make the contact area between the heat medium and the tubes larger, a plurality of baffles 30 with an angle of 30 to 45 degrees are installed in the heating chamber 102 to bend the flow direction of the heat exchange medium, so that the heat exchange medium provides heat to the tubes 20 in the form of baffles. Since the reaction system is sensitive to the change of reaction temperature, in order to make the reaction temperature in the segmented reactor 10 more uniform, the shell is divided into four sections (i.e., four heating chambers 102) to heat the tubes 20. Any two adjacent heating chambers 102 are separated by a partition 14, and a heat exchange medium inlet 104 and a heat exchange medium outlet 105 are provided on each heating chamber 102. Finally, the product gas after the catalyst reaction in the tubes 20 is cooled by the product heat exchanger 43 and discharged from the segmented reactor 10. In this way, by setting a plurality of sequentially connected heating chambers 102, heating of different regions in the length direction of the tubes 20 is achieved, so that the reaction degree in the tubes 20 in each heating chamber 102 can be adjusted as needed. By setting the baffle 30, the flow direction of the heat exchange medium in the heating chamber 102 is baffled, so that the heat exchange medium can be evenly heated to different positions in the length direction of the tubes 20 in the form of baffles, which is conducive to improving the removal efficiency and effect of oxides without increasing the isomerization rate of α-olefins.

[0045] Preferably, the Fischer-Tropsch synthetic oil includes components such as C6, C7, C8, C9, C10, C11, C12, C6-C7, C7-C8, C8-C9, C9-C10, C10-C11, C11-12, etc. The design pressure of the raw material preheater 42 is 0.1-3Mpa, the preheating temperature is 50-300°C, the design pressure of the staged reactor 10 is 0.1MPa-10Mpa, the reaction temperature is 40-400°C, and the space velocity of the reaction gas is 1-10h -1 The design pressure of the product heat exchanger 43 is 0.1-3Mpa, and the cooling temperature is 30-100℃.

[0046] In one specific embodiment, through simulation software, Fischer-Tropsch synthesis C10 is used as the reaction raw material, the raw material is heated to 145°C by the raw material pretreatment unit heater and enters the reactor, the gas phase C10 raw material enters the tube 20 filled with Co modified Al2O3 catalyst through the distributor 41 for reaction, and high-temperature steam is introduced into each section of the heating chamber 102 to control the temperature in the shell at 300°C, and the temperature difference of each heating chamber 102 is ±0.5°C. The product after the tube reaction is cooled to 70°C by the product heat exchanger 43 and discharged from the segmented reactor 10. After testing, the removal rate of oxides in the product is 95.8%, and the loss rate of α-olefins is 0.85%.

[0047] Comparative Example 1: The difference from the above specific embodiments is that the segmented reactor 10 is replaced with a traditional shell-and-tube reactor, the reactor is not segmented, and a single arched baffle installed at 90° is arranged inside. The removal rate of oxides in the product is tested to be 89.5%, and the loss rate of α-olefins is 2.3%.

[0048] Comparative Example 2: The difference from the above specific examples is that the segmented reactor 10 is replaced with a fixed bed reactor, and the reactor is not segmented. The removal rate of oxides in the product is detected to be 86.3%, and the loss rate of α-olefins is 0.8%.

[0049] Comparative Example 3: The difference from the above specific examples is that the segmented reactor 10 is replaced with a single tubular bed reactor. The removal rate of oxides in the product is detected to be 94.3%, and the loss rate of α-olefins is 5.8%.

[0050] By comparing the above specific embodiment with comparative embodiment 1, comparative embodiment 2, and comparative embodiment 3, it can be seen that the structure of the present invention is simple and the amplification effect is not obvious. The segmented reactor 10 and the baffle 30 provided in this embodiment realize multi-stage heating of different positions of the tube array 20, which is conducive to uniform temperature distribution and improves heat transfer efficiency. On the other hand, the distributor 41 is conducive to uniform distribution of gas phase Fischer-Tropsch synthesis oil in the catalyst, which is conducive to improving the contact effect and reaction efficiency with the metal catalyst, and is more suitable for reaction to remove oxides in Fischer-Tropsch synthesis oil.

[0051] It should be noted that the terms used herein are only for describing specific embodiments and are not intended to limit the exemplary embodiments according to the present application. As used herein, unless the context clearly indicates otherwise, the singular form is also intended to include the plural form. In addition, it should be understood that when the terms "comprise" and / or "include" are used in this specification, it indicates the presence of features, steps, operations, devices, components and / or combinations thereof.

[0052] Unless otherwise specifically stated, the relative arrangement of the parts and steps described in these embodiments, numerical expressions and numerical values ​​do not limit the scope of the present invention. At the same time, it should be understood that, for ease of description, the sizes of the various parts shown in the accompanying drawings are not drawn according to the actual proportional relationship. The technology, method and equipment known to ordinary technicians in the relevant field may not be discussed in detail, but in appropriate cases, the technology, method and equipment should be regarded as a part of the authorization specification. In all examples shown and discussed here, any specific value should be interpreted as being merely exemplary, rather than as a limitation. Therefore, other examples of exemplary embodiments may have different values. It should be noted that similar reference numerals and letters represent similar items in the following drawings, so once a certain item is defined in an accompanying drawing, it does not need to be further discussed in subsequent drawings.

[0053] In the description of the present invention, it is necessary to understand that the directions or positional relationships indicated by directional words such as "front, back, up, down, left, right", "lateral, vertical, perpendicular, horizontal" and "top, bottom" are usually based on the directions or positional relationships shown in the drawings. They are only for the convenience of describing the present invention and simplifying the description. Unless otherwise specified, these directional words do not indicate or imply that the devices or elements referred to must have a specific direction or be constructed and operated in a specific direction. Therefore, they cannot be understood as limiting the scope of protection of the present invention. The directional words "inside and outside" refer to the inside and outside relative to the contours of each component itself.

[0054] For ease of description, spatially relative terms such as "above", "above", "on the upper surface of", "above", etc. may be used here to describe the spatial positional relationship between a device or feature and other devices or features as shown in the figure. It should be understood that spatially relative terms are intended to include different orientations of the device in use or operation in addition to the orientation described in the figure. For example, if the device in the accompanying drawings is inverted, the device described as "above other devices or structures" or "above other devices or structures" will be positioned as "below other devices or structures" or "below other devices or structures". Thus, the exemplary term "above" can include both "above" and "below". The device can also be positioned in other different ways (rotated 90 degrees or in other orientations), and the spatially relative descriptions used here are interpreted accordingly.

[0055] In addition, it should be noted that the use of terms such as "first" and "second" to limit components is only for the convenience of distinguishing the corresponding components. If not otherwise stated, the above terms have no special meaning and therefore cannot be understood as limiting the scope of protection of the present invention.

[0056] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A reaction system for removing oxides from Fischer-Tropsch synthetic oil, characterized in that: The reaction system for removing oxides from Fischer-Tropsch synthesis oil comprises: A segmented reactor (10), wherein the segmented reactor (10) comprises a raw gas distribution chamber (101), a plurality of heating chambers (102) and a product chamber (103) which are sequentially spaced from top to bottom, any one of the heating chambers (102) having a heat exchange medium inlet (104) and a heat exchange medium outlet (105), and the Fischer-Tropsch synthesis oil raw gas to be deoxidized enters from the raw gas distribution chamber (101) and is finally discharged from the product chamber (103); A tube array (20), wherein the extending direction of the tube array (20) is parallel to the extending direction of the segmented reactor (10), the tube array (20) is multiple and is distributed at intervals in the segmented reactor (10), and the openings at both ends of any one of the tube arrays (20) extend to the raw gas distribution chamber (101) and the product chamber (103), respectively, and the tube array (20) is filled with a metal oxide catalyst; Baffles (30), wherein a plurality of baffles (30) inclined relative to a horizontal plane are arranged in any one of the heating chambers (102), the heat exchange medium inlet (104) is located above the uppermost baffle (30), and the plurality of baffles (30) are used to bend and guide the heat medium so that the heat medium flows through different axial positions of the plurality of tube arrays (20) during the falling process.

2. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 1, characterized in that: In the radial direction of the segmented reactor (10), one side of the baffle (30) is fixedly connected to the inner wall of the segmented reactor (10), and the other side of the baffle (30) at least extends downwardly in an inclined manner to the center line of the segmented reactor (10).

3. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 2, characterized in that: For any one of the heating chambers (102), the multiple baffles (30) therein are spaced apart along the axial direction of the segmented reactor (10), and any two adjacent baffles (30) are staggered in the circumferential direction of the segmented reactor (10), and the projections of the two baffles on the radial plane of the segmented reactor (10) on the side close to the center line of the segmented reactor (10) at least partially overlap.

4. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 3, characterized in that: For any one of the heating chambers (102), the projection centers of any two adjacent baffles (30) therein on the radial plane of the segmented reactor (10) are symmetrically arranged and cover the projection of the heating chamber (102) on the radial plane of the segmented reactor (10).

5. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 2, characterized in that: For any one of the heating chambers (102), the inclination angles of the multiple baffles (30) inside the chamber are the same.

6. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 5, characterized in that: The inclination angle of the baffle (30) is α=30° to 45°.

7. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The metal oxide catalyst is one or more of Al2O3, SiO2, TiO2, ZnO, Ga2O3, and MgO modified by one or more of Cu, Ni, Zn, Mg, Ca, and Co.

8. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The segmented reactor (10) comprises an upper head (11), a shell (12) and a lower head (13) connected in sequence from top to bottom; the cavity in the upper head (11) forms the raw gas distribution chamber (101); the cavity in the lower head (13) forms the product chamber (103); a plurality of partitions (14) are arranged in the shell (12) along its axial direction; the raw gas distribution chamber (101) and the heating chamber (102) adjacent thereto are separated by one of the partitions (14); the product chamber (103) and the heating chamber (102) adjacent thereto are separated by one of the partitions (14); the remaining partitions (14) are used to divide the shell (12) into a plurality of the heating chambers (102); and the openings at both ends of the tube array (20) extend to the two partitions (14) located at the two ends respectively.

9. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 8, characterized in that: The reaction system for removing oxides from Fischer-Tropsch synthetic oil also includes a distributor (41) arranged in the upper head (11), and the distributor (41) is externally connected to a feeding device to evenly distribute the gaseous raw material transported by the feeding device to the upper head (11) in the raw gas distribution chamber (101).

10. The reaction system for removing oxides from Fischer-Tropsch synthetic oil according to claim 9, characterized in that: The reaction system for removing oxides from Fischer-Tropsch synthetic oil also includes a raw material preheater (42) and a product heat exchanger (43). The raw material preheater (42) is arranged on an external pipeline between the feeding device and the distributor (41) to heat the raw material transported by the feeding device to make it gaseous. The product heat exchanger (43) is arranged on an external pipeline connected to the bottom of the lower head (13) to cool the discharged material.

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