Reaction device and system for hydrogenation and olefin removal of reformate and application of reaction device and system

Abstract

The invention belongs to the field of chemical engineering, and particularly relates to a reaction device and system for hydrodeolefination of reformate and application of the reaction device and system. The reaction device for hydrogenation and olefin removal of reformate comprises a cylinder, the cylinder comprises an inner cylinder and an annular reaction cavity located between the inner cylinder wall and the inner wall of the cylinder, and an annular catalyst bed layer is arranged in the annular reaction cavity; a cooling mechanism is arranged in the inner cylinder; a heating mechanism is arranged on the outer wall side of the barrel; the reaction device further comprises a feeding port and a feeding mechanism, wherein the feeding port and the feeding mechanism are located at the upper end of the barrel, and the feeding mechanism is used for conveying materials from the feeding port to the annular reaction cavity through multi-site feeding and / or rotary feeding. The reaction device further comprises a temperature detection mechanism used for being in contact with the annular catalyst bed layer. The reaction device can continuously carry out reformate hydrogenation reaction, maintain the dynamic balance of the temperature of the catalyst bed layer, better protect the catalyst and prolong the service life of the catalyst.

Description

Technical Field

[0001] This invention belongs to the field of chemical engineering, and specifically relates to a reaction apparatus, system and application for hydrodeolefination of reformate. Background Technology

[0002] Reformate is a petroleum intermediate product, primarily derived from C6-C11 naphtha fractions. In catalytic reforming units, these naphtha fractions undergo hydrocarbon molecule rearrangement under specific operating conditions and with the aid of catalysts, converting cycloalkanes and alkanes into aromatics or isoalkanes, thereby generating reformate.

[0003] The adsorbent used in the adsorption separation process of the isomerization unit in the aromatic hydrocarbon complex is very sensitive to olefins. Even if the content of olefin impurities is only a few parts per million, it will have a very adverse effect on the process.

[0004] Reformate contains a certain amount of unsaturated olefins, which seriously affects the stable operation and product quality of downstream aromatics complexes. Therefore, reformate typically requires pretreatment before entering downstream aromatics complexes. The main strategies for removing olefins from reformate include: clay adsorption, molecular sieve adsorption, and selective liquid-phase hydrogenation. Selective hydrogenation, due to its environmental friendliness and high efficiency, has become the mainstream trend for removing olefins from reformate. The hydrogenation reactor, as a crucial reaction device in selective hydrogenation, has a vital impact on the hydrogenation effect. Traditional hydrogenation reactors generally employ tubular fixed-bed hydrogenation reactors and batch hydrogenation reactors. While tubular fixed-bed hydrogenation reactors can achieve continuous reaction, they cannot effectively remove heat from the reaction in a timely manner, easily causing reactor overheating and catalyst damage. Although batch hydrogenation reactors can be equipped with internal cooling coils, the simultaneous stirring during the reaction affects catalyst stability, and the hydrogenation process is discontinuous. Summary of the Invention

[0005] The purpose of this invention is to address the shortcomings of existing hydrotreating reactors by providing a reaction apparatus, system, and application for the hydrotreating of reformate to remove olefins. Using the reaction apparatus, system, and method of this invention, reformate can be continuously hydrotreated, utilizing hydrogen to react with olefins in the reformate, reducing the olefin content and thus improving the quality of the reformate. Compared to the hydrotreating method in existing tubular fixed-bed hydrotreating reactors, the method of hydrotreating reformate to remove olefins using the apparatus and system of this invention allows for timely heating and cooling, maintaining the catalyst bed temperature within the target temperature range, achieving dynamic temperature equilibrium, avoiding runaway, and thus improving catalyst lifespan. Compared to the hydrotreating method in conventional batch hydrotreating reactors, the method of this invention enables continuous reaction and has higher production efficiency.

[0006] A first aspect of the present invention is to provide a reaction apparatus for hydrodeolefination of reformate, comprising a cylinder, the cylinder including an inner cylinder and an annular reaction chamber located between the inner cylinder wall and the inner wall of the cylinder, the annular reaction chamber being provided with an annular catalyst bed; a cooling mechanism is provided in the inner cylinder for cooling the annular reaction chamber; and a heating mechanism is provided on the outer wall side of the cylinder for heating the annular reaction chamber.

[0007] The reaction device also includes a feed inlet and a feeding mechanism located at the upper end of the cylinder. The feeding mechanism conveys the material from the feed inlet to the annular reaction chamber through multi-point feeding and / or rotary feeding.

[0008] The reaction apparatus also includes a temperature detection mechanism for contacting the annular catalyst bed.

[0009] Preferably, the feeding mechanism includes:

[0010] drive;

[0011] A receiver for receiving material from the feed inlet;

[0012] Multiple rotating fabric tubes located at the bottom of the receiver;

[0013] The receiver is used to drive the rotating feed tube to rotate under the drive of the driver, and to transport the material from the feed port to the annular reaction chamber through the rotating feed tube via multi-point feeding and / or rotating feeding.

[0014] Preferably, the receiver is an upward-opening container, the inlet is provided with a feed pipe, and the outlet end of the feed pipe is located above the receiver;

[0015] The rotating shaft of the driver is connected to the bottom of the receiver;

[0016] The bottom of the receiver is provided with multiple rotating material distribution pipes, the discharge end of the rotating material distribution pipes is located above the annular catalyst bed, and the driver is used to drive the receiver to rotate.

[0017] More preferably, the number of rotating fabric tubes is 2-8.

[0018] More preferably, the discharge ends of the rotating feed tube are evenly arranged above the annular catalyst bed.

[0019] Preferably, the cooling mechanism includes a refrigerant coil arranged along the inner wall of the inner cylinder, and the refrigerant coil has a refrigerant outlet and a refrigerant inlet through the outer wall of the cylinder.

[0020] More preferably, the refrigerant coil is spirally arranged along the inner wall of the inner cylinder.

[0021] More preferably, the refrigerant outlet and the refrigerant inlet are located at the lower end of the outer wall of the cylinder.

[0022] Preferably, the heating mechanism includes a heating jacket located on the outer wall side of the cylinder, the heating jacket being filled with a heat medium, and the heating jacket including a heat medium inlet and a heat medium outlet; more preferably,

[0023] The heat medium inlet is located at the lower end of the heating jacket, and the heat medium outlet is located at the upper end of the heating jacket.

[0024] Preferably, the temperature detection mechanism is a thermocouple; preferably, the thermocouple extends from bottom to top through the cylinder and contacts the annular catalyst bed.

[0025] Preferably, the cross-sectional area of ​​the inner cylinder accounts for 40%-75% of the cross-sectional area of ​​the cylinder body, more preferably 55%-65%.

[0026] Preferably, the bottom of the cylinder is provided with a discharge port.

[0027] Preferably, the catalyst in the annular catalyst bed is a hydrogenation catalyst.

[0028] A second aspect of the present invention is to provide a reaction system for hydrodeolefination of reformate, comprising:

[0029] A reaction apparatus, wherein the reaction apparatus is the reaction apparatus described in the first aspect;

[0030] A reforming oil source connected to the feed inlet of the reaction device;

[0031] A hydrogen source connected to the feed inlet of the reaction apparatus;

[0032] An annular hydrogenation catalyst bed is provided inside the annular reaction chamber;

[0033] Preferably, it further includes:

[0034] A cold source connected to the feed inlet of the cooling mechanism.

[0035] A heat medium source connected to the feed inlet of the heating mechanism.

[0036] A third aspect of the present invention is to provide a method for hydrodeolefination of reformate using the reaction system described in the second aspect, comprising:

[0037] The reforming oil and hydrogen are continuously reacted with the hydrogenation catalyst in the annular agent bed to obtain reforming oil with reduced olefin content.

[0038] The annular catalyst bed is heated by the heating mechanism, and during the continuous reaction process, the temperature of the catalyst bed is maintained within the target temperature range by cooling the annular catalyst bed to remove heat.

[0039] Preferably, the continuous reaction process is carried out under the temperature detection of a temperature detection mechanism.

[0040] A fourth aspect of the present invention is to provide an application of the reaction apparatus described in the first aspect, or the reaction system described in the second aspect, or the method described in the third aspect in the chemical industry.

[0041] Beneficial effects:

[0042] The reaction apparatus, system, and method of this invention enable continuous hydrogenation of reformate, utilizing hydrogen to react with olefins in the reformate, thereby reducing the olefin content and improving the quality of the reformate. Compared to existing hydrogenation methods in tubular fixed-bed hydrogenation reactors, the method of hydrogenating reformate to remove olefins using the apparatus and system of this invention allows for timely heating and cooling, maintaining the catalyst bed temperature within the target temperature range and achieving dynamic temperature equilibrium. This avoids runaway temperatures and improves catalyst lifespan. Compared to conventional hydrogenation methods in batch hydrogenation reactors, the method of this invention enables continuous reaction and has higher production efficiency.

[0043] The aforementioned technical effects are related to the specially designed reaction apparatus of this invention: Compared with traditional technologies, this invention changes the catalyst bed from a tubular filling to a ring-shaped filling, thereby providing space for the internal cooling coil. On the one hand, the larger contact area between the ring-shaped catalyst bed and the heating jacket enables rapid heating of the ring-shaped catalyst bed, increasing the heating rate. On the other hand, the shorter heat conduction distance allows for more efficient utilization of heat, reducing heat loss and lowering production costs. Furthermore, the cooling coil inside the reactor can promptly cool and extract heat from the exothermic reaction, achieving dynamic temperature balance in the catalyst bed, better protecting the catalyst and extending its lifespan. The specific design of the feed inlet and feeding mechanism not only creatively ensures uniform feeding of the ring-shaped catalyst bed but also guarantees a dynamically uniform temperature distribution, thus ensuring a stable reaction. Attached Figure Description

[0044] Figure 1 This is a front view of the reaction device in a specific embodiment of the present invention;

[0045] Figure 2 This is a top view of the reaction device in a specific embodiment of the present invention;

[0046] 1 is the reaction feed inlet.

[0047] 2 is the drive motor

[0048] 3 is the receiver

[0049] 4 is a rotating fabric tube

[0050] 5 is a ring-shaped catalyst bed

[0051] 6 is a heating jacket

[0052] 7 is the heat transfer medium import.

[0053] 8 is the refrigerant outlet.

[0054] 9 is a thermocouple

[0055] 10 is the outlet for heat transfer media.

[0056] 11 is the refrigerant coil.

[0057] 12 is for refrigerant import.

[0058] 13 is the reaction outlet. Detailed Implementation

[0059] The present invention will now be described in detail with reference to specific embodiments. It should be noted that the following embodiments are only used to further illustrate the present invention and should not be construed as limiting the scope of protection of the present invention. Some non-essential improvements and adjustments made by those skilled in the art based on the content of the present invention are still within the scope of protection of the present invention.

[0060] As previously described, the present invention provides a reaction apparatus for hydrodeolefination of reformate, comprising a cylinder, the cylinder including an inner cylinder and an annular reaction chamber located between the inner cylinder wall and the inner wall of the cylinder, the annular reaction chamber being provided with an annular catalyst bed; a cooling mechanism is provided in the inner cylinder for cooling the annular reaction chamber; a heating mechanism is provided on the outer wall side of the cylinder for heating the annular reaction chamber; the reaction apparatus further includes a feed inlet and a feeding mechanism located at the upper end of the cylinder, the feeding mechanism conveying material from the feed inlet to the annular reaction chamber through multi-point feeding and / or rotary feeding; the reaction apparatus further includes a temperature detection mechanism for contacting the annular catalyst bed. In this way, by changing the catalyst bed from a tubular packing to a ring packing, space is provided for a cooling mechanism inside the inner cylinder. The reactants undergo hydrogenation at the ring catalyst bed, and the heating mechanism directly heats the ring catalyst bed within the annular reaction chamber. This increases the heating rate while reducing energy loss and lowering production costs. During the exothermic hydrogenation reaction, to effectively control runaway temperatures and stabilize the bed temperature to protect the catalyst, when the temperature detection mechanism detects heat release or runaway temperatures inside the reactor, the cooling mechanism promptly cools and removes heat from the annular catalyst bed inside the reactor, achieving dynamic temperature balance and better protecting the catalyst. The specific design of the feed inlet and feed mechanism described above not only creatively ensures uniform feeding of the annular catalyst bed but also guarantees a dynamically uniform temperature distribution, thus ensuring a stable reaction.

[0061] The reaction apparatus of this invention can also be called a reactor. For example... Figure 1 As shown, the reaction apparatus of the present invention is vertical.

[0062] According to some preferred embodiments of the present invention, the feeding mechanism includes: a driver; a receiver for receiving material from the feed inlet; and a plurality of rotating feed tubes located at the bottom of the receiver. The receiver is used to drive the rotating feed tubes to rotate under the drive of the driver, and to transport the material from the feed inlet to the annular reaction chamber through the rotating feed tubes via multi-point feeding and / or rotating feeding. By setting the periodic rotation frequency of the driver, the receiving and uniform conveying of the incoming material is achieved. This ensures that the hydrogenation material can uniformly wet the catalyst bed, and all materials undergo sufficient hydrogenation reaction.

[0063] According to some preferred embodiments of the present invention, the receiver is an upward-opening container, the inlet is provided with a feed pipe, and the outlet end of the feed pipe is located above the receiver; the rotating shaft of the driver is connected to the bottom of the receiver; the bottom of the receiver is provided with multiple rotating distribution pipes, the outlet ends of the rotating distribution pipes are located above the annular catalyst bed, and the driver is used to drive the receiver to rotate. Thus, by adopting the above specific embodiments, the receiving of incoming materials is more ingeniously implemented through simple components, and the incoming materials are uniformly transported to the novel annular catalyst bed through rotation and mechanical control, which can further improve working efficiency.

[0064] According to the present invention, preferably, the driver is a motor.

[0065] According to some preferred embodiments of the present invention, the number of rotating feed tubes is 2-8; and / or, the outlet ends of the rotating feed tubes are evenly arranged above the annular catalyst bed. This makes the feeding more uniform.

[0066] According to the present invention, preferably, the reaction apparatus of the present invention includes a cylindrical body, an upper end cap disposed at the upper end of the cylindrical body, and a lower end cap disposed at the lower end of the cylindrical body. More preferably, the upper end cap and the lower end cap are detachably connected to the cylindrical body.

[0067] The present invention does not impose any particular restrictions on the shape of the upper and lower end caps. For example, they can be one of the following: hemispherical end cap, elliptical end cap, butterfly end cap, etc. Preferably, the upper end cap is a butterfly end cap.

[0068] More preferably, the receiver, the rotating feed tube, and part of the feed tube are all disposed in the cavity of the upper end cap.

[0069] According to some preferred embodiments of the present invention, the cooling mechanism includes a refrigerant coil arranged along the inner wall of the inner cylinder, and the refrigerant coil has a refrigerant outlet and a refrigerant inlet through the outer wall of the cylinder. Thus, when runaway temperatures occur during the hydrotreating of reformate, the timely entry of the refrigerant and its external heat extraction helps maintain the stability of the catalyst bed temperature and protects the catalyst.

[0070] According to some preferred embodiments of the present invention, the refrigerant coil is spirally arranged along the inner wall of the inner cylinder. This spiral arrangement of the refrigerant coil fully utilizes the space within the inner cylinder, and the larger cooling area facilitates heat exchange, enabling rapid temperature control.

[0071] Preferably, when the refrigerant coil is spirally arranged to the upper part of the inner cylinder, it begins to spiral downwards from the top in a structure similar to a DNA double helix, and finally exits from the lower end of the outer wall of the cylinder. The refrigerant outlet and the refrigerant inlet are located at the lower end of the outer wall of the cylinder. In this way, if the cooling system fails, it is convenient to remove the cooling system directly from the lower end cap of the reaction device, facilitating replacement of spare parts and simplifying operation.

[0072] Preferably, the spiral arrangement of the refrigerant coil starts from the connection between the lower end cap and the cylinder, and its height is flush with the catalyst bed. This facilitates timely control of the temperature of the entire catalyst bed.

[0073] According to some preferred embodiments of the present invention, the heating mechanism includes a heating jacket located on the outer wall side of the cylinder, the heating jacket being filled with a heating medium, and the heating jacket including a heating medium inlet and a heating medium outlet. Thus, the larger contact area of ​​the heating jacket enables rapid heating of the annular catalyst bed, and the shorter heat conduction distance allows for more efficient utilization of the heat.

[0074] Preferably, the heating jacket is positioned from the lower end cap connection to the upper end cap connection, and its height is slightly higher than the catalyst bed. This facilitates sufficient heat supply and allows for steady heating of the entire catalyst bed.

[0075] According to some preferred embodiments of the present invention, the heat medium inlet is located at the lower end of the heating jacket, and the heat medium outlet is located at the upper end of the heating jacket. This bottom-in, top-out configuration facilitates the full filling of the heat medium cavity, resulting in a more uniform heating effect.

[0076] According to some preferred embodiments of the present invention, the temperature detection mechanism is a thermocouple.

[0077] According to some preferred embodiments of the present invention, the thermocouple sheath is welded and fixed to the lower end cap, penetrating the cylinder from bottom to top and contacting the annular catalyst bed. In this way, extending the thermocouple into the thermocouple sheath allows access to the catalyst bed, facilitating timely measurement of the catalyst bed temperature.

[0078] According to some preferred embodiments of the present invention, the cross-sectional area of ​​the inner cylinder accounts for 40%-75% of the cross-sectional area of ​​the cylinder body, preferably 55%-65%. Thus, when the cross-sectional area of ​​the inner cylinder accounts for about half of the total cross-sectional area of ​​the cylinder body, the heating effect is optimal, the thermal efficiency is relatively high, and it is also more conducive to timely heat dissipation.

[0079] According to some preferred embodiments of the present invention, a discharge port is provided at the bottom of the cylinder.

[0080] According to some preferred embodiments of the present invention, the catalyst in the annular catalyst bed is a hydrogenation catalyst. The present invention does not impose any particular limitation on the hydrogenation catalyst; any catalyst suitable for the hydrodeolefination reaction of reformate can be used to implement the present invention. The present invention is applicable to both catalysts with high and low temperature control requirements.

[0081] According to a preferred embodiment of the present invention, the upper end of the inner cylinder is sealed, while the lower end is unsealed. Sealing the upper end prevents hydrogen and reformate from exiting the inner cylinder directly without passing through the catalyst bed. By sealing the upper end of the inner cylinder, hydrogen and reformate can only pass through the catalyst bed, facilitating the hydrogenation reaction. Leaving the lower end unsealed facilitates the removal of the cooling coil. In the event of a cooling system malfunction, the cooling system can be easily removed directly from the lower end of the reaction unit, facilitating replacement of spare parts and simplifying operation.

[0082] To facilitate understanding of the present invention, a specific preferred embodiment is provided, such as... Figure 1 , Figure 2 As shown, a reactor for hydrodeolefins treatment of reformed oil includes a cylindrical body, which comprises an inner cylinder and an annular reaction chamber located between the inner cylinder wall and the inner wall of the cylindrical body. An annular catalyst bed 5 is disposed within the annular reaction chamber. The reactor also includes a reaction inlet 1, a drive motor 2, a receiver 3, rotating distribution pipes 4, a heating jacket 6, a heat transfer medium inlet 7, a refrigerant outlet 8, a thermocouple 9, a heat transfer medium outlet 10, a refrigerant coil 11, a refrigerant inlet 12, and a reaction outlet 13. The reaction feedstock, reformed oil and hydrogen, is pumped into the receiver 3 through the reaction inlet 1. The receiver 3 is connected to 2-8 rotating distribution pipes 4. The periodic rotation of the drive motor 2 drives the receiver 3 and the rotating distribution pipes 4 to rotate and distribute the liquid. The distribution rate and distribution point are periodically controlled by the motor frequency. The reactants undergo hydrogenation at the annular catalyst bed 5. During the exothermic hydrogenation reaction, the motor rotation frequency, liquid distribution rate, and liquid distribution point are periodically regulated by the motor frequency to ensure that the catalyst bed can be completely wetted with the material and hydrogenated. The reactants undergo hydrogenation at the annular catalyst bed.

[0083] The large contact area between the annular catalyst bed 5 and the heating jacket 6 enables rapid heating of the annular catalyst bed 5. While increasing the heating rate, the shorter heat conduction distance allows for more efficient heat utilization, reducing energy loss and lowering production costs.

[0084] During the hydrogenation reaction, by observing the catalyst bed temperature, when the reactor releases heat and the temperature rises, the annular catalyst bed 5 inside the reactor is cooled and heated in time by introducing coolant through the coolant coil 11 set in the inner cylinder, so as to achieve dynamic balance of catalyst bed temperature.

[0085] A second aspect of the present invention is to provide a reaction system for hydrodeolefination of reformate, comprising:

[0086] The reaction apparatus is the same as described in the first aspect; a reforming oil source connected to the feed inlet of the reaction apparatus; a hydrogen source connected to the feed inlet of the reaction apparatus; and an annular hydrogenation catalyst bed is provided inside the annular reaction chamber.

[0087] Preferably, before entering the reaction device, hydrogen and reformed oil are combined into a single feed stream and enter the annular reaction chamber from the feed inlet of the reaction device for reaction.

[0088] According to some more preferred embodiments of the present invention, it further includes a cold source connected to the feed inlet of the cooling mechanism, wherein the cold source may be cooling water, ethylene glycol, etc.

[0089] According to some preferred embodiments of the present invention, a heat medium source is connected to the feed inlet of the heating mechanism. The heat medium source can be heat transfer oil, steam, etc.

[0090] The present invention does not have any particular limitation on the hydrogenation catalyst used in the annular hydrogenation catalyst bed. Any catalyst suitable for hydrogenating reformate to obtain reformate with reduced olefin content can be used to realize the present invention.

[0091] A third aspect of the present invention is to provide a method for hydrodeolefination of reformate using the reaction system described in the second aspect, comprising:

[0092] The reforming oil and hydrogen are continuously reacted with the hydrogenation catalyst in the annular agent bed to obtain reforming oil with reduced olefin content.

[0093] The annular catalyst bed is heated by the heating mechanism, and during the continuous reaction process, the temperature of the catalyst bed is maintained within the target temperature range by cooling the annular catalyst bed to remove heat.

[0094] This invention enables continuous hydrogenation of reformate, utilizing hydrogen to react with olefins in the reformate, thereby reducing the olefin content and improving the quality of the reformate. Compared to existing tubular fixed-bed hydrogenation reactors, the apparatus and system of this invention allow for timely heating and cooling, maintaining the catalyst bed temperature within the target range and achieving dynamic temperature equilibrium. Compared to conventional batch hydrogenation reactors, this invention enables continuous reaction and offers higher production efficiency.

[0095] According to some preferred embodiments of the present invention, the continuous reaction process is carried out under the temperature detection of a temperature detection mechanism.

[0096] A fourth aspect of the present invention is to provide an application of the reaction apparatus described in the first aspect, or the reaction system described in the second aspect, or the method described in the third aspect in the chemical industry.

[0097] As mentioned above, this invention enables continuous hydrogenation of reformate, utilizing hydrogen to react with olefins in the reformate, thereby reducing the olefin content and improving the quality of the reformate. Compared to existing tubular fixed-bed hydrogenation reactors, the device and system of this invention allow for timely heating and cooling, maintaining the catalyst bed temperature within the target range and achieving dynamic temperature equilibrium. Compared to conventional batch hydrogenation reactors, this invention enables continuous reaction, resulting in higher production efficiency and significant potential for widespread application.

[0098] It should be noted that the embodiments described above are only for explaining the present invention and do not constitute any limitation on the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory terms, not limiting terms. Modifications can be made to the present invention within the scope of the claims, and revisions can be made to the present invention without departing from the scope and spirit of the present invention. Although the present invention described herein relates to specific methods, materials, and embodiments, it does not mean that the present invention is limited to the specific examples disclosed herein; on the contrary, the present invention can be extended to all other methods and applications with the same function.

[0099] All publications, patent applications, patents, and other references mentioned in this specification are incorporated herein by reference. Unless otherwise defined, all technical and scientific terms used in this specification have the meanings commonly understood by those skilled in the art. In case of conflict, the definitions in this specification shall prevail.

[0100] When this specification uses the prefixes “known to those skilled in the art,” “prior art,” or similar terms to derive materials, substances, methods, steps, apparatus, or components, the objects derived from such prefixes cover those commonly used in the art at the time of this application’s filing, but also include those that are not currently commonly used but will become generally recognized in the art as suitable for similar purposes.

[0101] The endpoints and any values ​​of the ranges disclosed in this application are not limited to the precise ranges or values; such ranges or values ​​should be understood to include values ​​close to them. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein. In principle, various technical solutions can be combined with each other to obtain new technical solutions, which should also be considered as specifically disclosed herein.

[0102] In the context of this specification, except where expressly stated otherwise, any matters or issues not mentioned shall apply directly to those known in the art without any modification.

[0103] Furthermore, any implementation described herein can be freely combined with one or more other implementations described herein, and the resulting technical solutions or technical ideas shall be regarded as part of the original disclosure or original record of the present invention, and should not be regarded as new content not disclosed or anticipated herein, unless those skilled in the art consider the combination to be obviously unreasonable.

Claims

1. A reaction apparatus for hydrodeolefination of reformate, comprising a cylinder, the cylinder including an inner cylinder and an annular reaction chamber located between the inner cylinder wall and the inner wall of the cylinder, the annular reaction chamber being provided with an annular catalyst bed; a cooling mechanism is provided in the inner cylinder for cooling the annular reaction chamber; a heating mechanism is provided on the outer wall side of the cylinder for heating the annular reaction chamber; The reaction apparatus further includes a feed inlet and a feeding mechanism located at the upper end of the cylinder. The feeding mechanism is used to convey the material from the feed inlet to the annular reaction chamber through multi-point feeding and / or rotary feeding. The reaction apparatus also includes a temperature detection mechanism for contacting the annular catalyst bed.

2. The reaction apparatus according to claim 1, characterized in that: The feeding mechanism includes: drive; A receiver for receiving material from the feed inlet; Multiple rotating fabric tubes located at the bottom of the receiver; The receiver is used to drive the rotating feed tube to rotate under the drive of the driver, and to transport the material from the feed port to the annular reaction chamber through the rotating feed tube via multi-point feeding and / or rotating feeding.

3. The reaction apparatus according to claim 2, characterized in that: The receiving device is an upward-opening container, the inlet is provided with a feeding pipe, and the outlet end of the feeding pipe is located above the receiving device; The rotating shaft of the driver is connected to the bottom of the receiver; The bottom of the receiver is provided with multiple rotating material distribution pipes, the discharge end of the rotating material distribution pipes is located above the annular catalyst bed, and the driver is used to drive the receiver to rotate. Preferably, the number of rotating fabric tubes is 2-8; and / or, The discharge ends of the rotating feed pipe are evenly arranged above the annular catalyst bed.

4. The reaction apparatus according to claim 1, characterized in that: The cooling mechanism includes a refrigerant coil arranged along the inner wall of the inner cylinder, and the refrigerant coil has a refrigerant outlet and a refrigerant inlet through the outer wall of the cylinder. Preferably, the refrigerant coil is spirally arranged along the inner wall of the inner cylinder; and / or, Preferably, the refrigerant outlet and the refrigerant inlet are located at the lower end of the outer wall of the cylinder.

5. The reaction apparatus according to claim 1, characterized in that: The heating mechanism includes a heating jacket located on the outer wall side of the cylinder, the heating jacket being filled with a heat medium, and the heating jacket including a heat medium inlet and a heat medium outlet; preferably, The heat medium inlet is located at the lower end of the heating jacket, and the heat medium outlet is located at the upper end of the heating jacket.

6. The reaction apparatus according to claim 1, characterized in that: The temperature detection mechanism is a thermocouple; preferably, the thermocouple extends from bottom to top through the cylinder and contacts the annular catalyst bed.

7. The reaction apparatus according to any one of claims 1-6, characterized in that: The cross-sectional area of ​​the inner cylinder accounts for 40%-75% of the cross-sectional area of ​​the cylinder body, preferably 55%-65%; and / or, The bottom of the cylinder is provided with a discharge port; and / or, The catalyst in the annular catalyst bed is a hydrogenation catalyst.

8. A reaction system for hydrodeolefination of reformate, comprising: A reaction apparatus, wherein the reaction apparatus is the reaction apparatus according to any one of claims 1-7; A reforming oil source connected to the feed inlet of the reaction device; A hydrogen source connected to the feed inlet of the reaction apparatus; An annular hydrogenation catalyst bed is provided inside the annular reaction chamber; Preferably, it further includes: A cold source connected to the feed inlet of the cooling mechanism; and / or, A heat medium source connected to the feed inlet of the heating mechanism.

9. A method for hydrodeolefination of reformate using the reaction system of claim 8, comprising: The reforming oil and hydrogen are continuously reacted with the hydrogenation catalyst in the annular agent bed to obtain reforming oil with reduced olefin content. The annular catalyst bed is heated by the heating mechanism, and during the continuous reaction process, the temperature of the catalyst bed is maintained within the target temperature range by cooling the annular catalyst bed to remove heat. Preferably, the continuous reaction process is carried out under the temperature detection of a temperature detection mechanism.

10. The application of a reaction apparatus according to any one of claims 1-7, or a reaction system according to claim 8, or a method according to claim 9 in the chemical industry.

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