Alkylation reaction device

Abstract

The utility model provides an alkylation reaction device and method. The device comprises a reactor, and three strengthening units are vertically arranged in the reactor; the first strengthening unit is arranged at the bottom of the reactor, the second strengthening unit is arranged right above the first strengthening unit, and the third strengthening unit is arranged in the middle of the reactor; a sensor is also arranged in the reactor, clings to the inner wall of the reactor, and is positioned above the third strengthening unit; a main pipeline is arranged at the top of the reactor. The reaction device can improve the reaction efficiency and the product purity, reduce the reaction energy consumption and prolong the service life of equipment.

Description

Technical Field

[0001] The present invention belongs to the technical field of chemical engineering, and more specifically, to an alkylation reaction device. Background Art

[0002] Alkylation reaction is an important type of organic reaction. Through alkylation, new covalent bonds such as carbon-carbon and carbon-heteroatom bonds can be formed, thereby extending the molecular skeleton of organic compounds, changing the chemical structure of the alkylated substances, endowing them with new properties, and manufacturing many organic chemicals with specific uses. In traditional processes, due to the low solubility between reactants and catalysts, the reaction efficiency decreases, and at the same time, it is difficult to recycle the catalysts and remaining reactants, resulting in waste.

[0003] In view of this, the present invention is specifically proposed. Utility Model Content

[0004] The first object of the present invention is to provide an alkylation reaction device. This reaction device, through double circulation and internal circulation pipelines and supporting devices, improves the reaction efficiency and the purity of the product, reduces the reaction energy consumption, and at the same time can effectively recycle the catalyst and the remaining reactants; and is equipped with an intelligent control system to control the reaction device.

[0005] The second object of the present invention is to provide the reaction method for the above alkylation reaction. This reaction method can cooperate with the reaction device, simplify the reaction process, and improve the reaction efficiency.

[0006] To achieve the above objects of the present invention, the following technical solutions are specifically adopted:

[0007] The present invention provides an alkylation reaction device, comprising:

[0008] A reactor, inside which three intensifying units are vertically arranged;

[0009] The first intensifying unit is arranged at the bottom of the reactor, the second intensifying unit is arranged directly above the first intensifying unit, and the third intensifying unit is arranged in the middle of the reactor;

[0010] A sensor is also arranged inside the reactor. The sensor is closely attached to the inner wall of the reactor and is located above the third intensifying unit;

[0011] A main pipeline is arranged at the top of the reactor.

[0012] In the present invention, a first intensifying unit is provided, which can break and disperse the gaseous reactants introduced therein; a second intensifying unit arranged directly above the first intensifying unit is used to mix and disperse the catalyst and the reaction liquid introduced therein. The broken gas ascends and is fully mixed with the catalyst and the reaction liquid that have been broken and dispersed, and a reaction occurs to generate reactants. Since in the actual reaction process, incomplete reactions may occur, in the present invention, some incompletely reacted reactants can continue to react through the third intensifying unit, enabling the reactants to react fully, thereby making the reaction more complete and solving the technical problems proposed by the present invention.

[0013] In the present invention, the positions of the respective intensifying units are defined. In the present invention, the first intensifying unit should be arranged at the bottom of the reactor. When the first intensifying unit is arranged at the bottom of the reactor, the broken gas can escape and enter the second intensifying unit, causing the gas to collide therein. When the positions of the two intensifying units are changed, the reaction is difficult to occur. Moreover, in the present invention, the position of the third intensifying unit is defined. The third intensifying unit is located in the middle of the reactor. The reason is that at this time, the reacted reactants continuously ascend after being broken and reacted, and there is a large amount of gas in the middle of the reactor. When the third intensifying unit is arranged at this position, not only can as much unreacted gas as possible participate in the reaction; at the same time, the sensor arranged above the third intensifying unit can also better detect the state inside the reactor after passing through the third intensifying unit, improving the reaction efficiency and also playing a role in accurate detection. Finally, when the third intensifying unit is arranged in the middle of the reactor, it can also ensure that the reactants passing through the first circulation pipeline are not sucked into the second intensifying unit to cause by-products.

[0014] Meanwhile, due to the setting of the intensifying unit, the reaction temperature inside the reactor can be well reduced, achieving the purpose of accelerating the reaction process and reducing energy consumption.

[0015] A sensor is also arranged in the reactor of the present invention. The sensor should be arranged above the third intensifying unit. The sensor is used to detect the content of each substance in the reactor after complete reaction to confirm the reaction situation, and feedback the reaction situation in the reactor, and control the control valve according to the reaction situation to realize the control of the reaction process.

[0016] The main pipeline is connected to the first circulation pipeline and the second circulation pipeline in a parallel manner;

[0017] The first circulation pipeline is connected to the second circulation pipeline to form an internal circulation, and a circulation pump is arranged on the internal circulation pipeline;

[0018] Control valves a and b are respectively arranged at the connection points of the first circulation pipeline and the second circulation pipeline;

[0019] The outlet of the first circulation pipeline is connected to the third intensifying unit.

[0020] In the present invention, through the arrangement of the first circulation pipeline and the second circulation pipeline, the reactants that have not participated in the reaction can be fully reacted, the reaction efficiency can be improved, and the recovery of the catalyst can be realized. The sensor located above the third intensifying unit detects the environment inside the reactor. When the sensor detects that there are a large number of unreacted reactants inside the reactor, at this time, the controller turns on the circulation pump to provide power for the reactants in the circulation pipeline, and closes the control valve a and the control valve b, so that the reaction liquid circulates once on the internal circulation pipeline, and the unreacted reactants use the waste heat during the reaction process to react and disperse; after one circulation is completed, the circulation pump is turned off and the control valve a is opened, so that the reactants are broken and mixed again in the third intensifying unit for reaction to obtain the product. Subsequently, the controller controls the control valve a to close and the control valve b to open, so that the product enters the second circulation pipeline for subsequent separation.

[0021] During the actual reaction process, due to the existence of the internal circulation pipeline, the internal circulation pipeline, the first circulation pipeline, and the second circulation pipeline are all only opened once, and after one time, it can be ensured that the reactants participating in the reaction are fully reacted. When the circulation pipeline is opened two or more times, it will cause excessive reaction and increase the content of by-products. Therefore, in the present invention, only one circulation can ensure the complete reaction of the reactants, so as to achieve the purpose of energy conservation and reduction of by-products.

[0022] In addition, the outlet of the first circulation pipeline is connected to the third intensifying unit and cannot be connected to other intensifying units. The reason is that the reactants participating in the reaction need other mechanical devices to provide power, and the third intensifying unit can form a low-pressure area to generate suction on the substances in the pipeline, so that the substances participating in the reaction in the pipeline quickly enter the reaction system again and complete the reaction quickly. And the outlet of the first circulation pipeline cannot be connected to the second intensifying unit. The reason is that at the end of the first reaction, there are a large number of products and a small amount of unreacted reactants in the pipeline at this time. When the first circulation pipeline is connected to the second intensifying unit, a large number of products and a small amount of reactants continue to pass upward through the third intensifying unit after passing through the second intensifying unit. After two reactions, it will cause excessive reaction, and a large number of products will undergo side reactions, thereby reducing the reaction efficiency, which is contrary to the original intention of the set circulation pipeline.

[0023] The second circulation pipeline is connected to the separation device;

[0024] The separation device is connected to the storage tank.

[0025] After the reaction is completed, the reactants are separated by a separation device. Different alkylation reactions use different separation devices. The separation device can be one or multiple, and can be selected according to actual needs. After passing through the separation device, the catalyst and reactants can be returned to the corresponding storage tanks for reuse, and the recovery of the catalyst and unutilized reactants can be achieved.

[0026] Preferably, as a further specific embodiment, a guiding port is provided above the first intensifying unit, and a baffle is provided above the guiding port.

[0027] Since the first intensifying unit is connected to the gas storage tank, the guiding port and baffle above the first intensifying unit can cause the gas entering the intensifying unit to collide and impinge, making the gas more dispersed, thus making the reaction more complete and improving the reaction efficiency.

[0028] Preferably, as a further specific embodiment, the alkylation reaction device further includes a catalyst storage tank, a gas storage tank and a liquid storage tank;

[0029] The gas storage tank is directly connected to the first intensifying unit through a gas pipeline, and a gas pipeline control valve is provided on the gas pipeline;

[0030] The catalyst storage tank provides a catalyst through a catalyst pipeline control valve on the catalyst pipeline, the liquid storage tank provides a reaction solution through a liquid pipeline control valve on the liquid pipeline, the catalyst pipeline and the liquid pipeline are connected in parallel to form a mixing pipeline, and the mixing pipeline is directly connected to the second intensifying unit.

[0031] The catalyst and the reaction solution enter the mixing pipeline, so that the catalyst and the reaction solution are premixed once in the mixing pipeline, and the two liquids after premixing enter the second intensifying unit, which can make the mixing more complete and uniform.

[0032] Preferably, control valves are provided in the pipelines of the alkylation reaction device, and the reaction state is controlled by the opening and closing and flow rate of the control valves.

[0033] Preferably, as a further specific embodiment, the alkylation reaction device further includes a controller, which can display the data transmitted from the sensors in real time and can control all the control valves in the alkylation reaction device through the controller.

[0034] The position and type of the control valves can be adjusted according to the different reactants actually participating in the reaction. Some devices (such as heat exchangers, etc.) on the reaction pipeline of the present invention can also be set according to actual reaction needs. The control valves selected in the present invention can control the opening and closing of the pipeline and can adjust the flow rate of the substances in the pipeline.

[0035] The present invention also provides a reaction method for an alkylation reaction device, comprising:

[0036] First, mixing the catalyst with the reaction solution, and then mixing with a gas for enhanced reaction to obtain the product.

[0037] When the alkylation reaction is the preparation of high-octane alkylated gasoline from isobutane and butene, the catalyst is a liquid catalyst.

[0038] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0039] (1) By setting up the first circulation pipeline and sensors, the state of the reactants in the reactor can be detected, and the unreacted reactants can be timely re-fed into the reaction system, improving the reaction efficiency. At the same time, the situation of overreaction is avoided, ensuring the purity of the product. By setting up the second circulation pipeline, the ionic liquid can be recovered, realizing the recovery of the liquid catalyst. Meanwhile, an internal circulation pipeline is set up, which can premix some of the unreacted reactants once, and the premixed reactants enter the reaction system again, improving the reaction efficiency and reducing energy consumption.

[0040] (2) By setting up the enhanced unit, the reactants and the catalyst can be fully mixed and dispersed, improving the reaction efficiency; at the same time, by setting up the guiding port and the baffle, the gases participating in the reaction can fully collide and impact, further improving the reaction efficiency.

[0041] (3) The reaction device realizes the recovery of the unreacted reactants and the catalyst. The settings of the sensors and the controller enable the reaction to proceed automatically, providing real-time feedback on the situation inside the reactor, ensuring the safety of the reaction in the reactor while improving the reaction efficiency. Description of the Drawings

[0042] Figure 1 : Diagram of the device for preparing high-octane alkylated gasoline by the alkylation reaction of isobutane and butene. Among them:

[0043] 1 - Reactor; 2 - Sensor; 3 - Controller; 4 - Third enhanced unit; 5 - Second enhanced unit;

[0044] 6 - Guiding port; 7 - Ionic liquid storage tank; 8 - Liquid storage tank; 9 - Baffle; 10 - Gas storage tank;

[0045] 11 - Ionic liquid pipeline control valve; 12 - Liquid pipeline control valve; 13 - Gas pipeline control valve;

[0046] 14 - Control valve e; 15 - First enhanced unit; 16 - Control valve b; 17 - Control valve a;

[0047] 18 - Circulation pump; 19 - Separation device; 20 - Phase separator; 21 - Control valve c; 22 - Control valve d.

[0048] Figure 2 : Diagram of the device for the reaction of ethylene and benzene to produce ethylbenzene. Among them:

[0049] 101 - Reactor; 102 - Controller; 103 - Sensor; 104 - Third intensification unit;

[0050] 105 - Second intensification unit; 106 - Baffle; 107 - Guide port; 108 - First intensification unit;

[0051] 109 - Gas pipeline control valve; 110 - Gas storage tank; 111 - Heat exchanger; 112 - Circulation pump;

[0052] 113 - Control valve a; 114 - Control valve b; 115 - Distillation column; 116 - Catalyst storage tank;

[0053] 117 - Liquid storage tank; 118 - Catalyst pipeline control valve; 119 - Liquid pipeline control valve;

[0054] 120 - Control valve e; 121 - Control valve f; 122 - Control valve g. Specific implementation mode

[0055] The technical solutions of the present invention will be clearly and completely described below in conjunction with the accompanying drawings and specific implementation modes. However, those skilled in the art will understand that the following described embodiments are part of the embodiments of the present invention, rather than all of the embodiments, and are only used to illustrate the present invention and should not be construed as limiting the scope of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without making creative efforts belong to the scope of protection of the present invention. For those conditions not specified in the embodiments, they are carried out according to conventional conditions or conditions recommended by the manufacturer. Those reagents or instruments not specified by the manufacturer can be obtained as conventional products through commercial purchase.

[0056] In the description of the present invention, it should be noted that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc. is based on the orientation or positional relationship shown in the accompanying drawings, and is only for the convenience of describing the present invention 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 construed as a limitation of the present invention. In addition, the terms "first", "second", "third" are only used for descriptive purposes and cannot be construed as indicating or implying relative importance.

[0057] In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, the terms "installed", "connected", and "coupled" should be understood in a broad sense. For example, it may be a fixed connection, a detachable connection, or an integral connection; it may be a mechanical connection or an electrical connection; it may be directly connected or indirectly connected through an intermediate medium, and it may be the communication inside two components. For those of ordinary skill in the art, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0058] Example 1

[0059] Preparation of high-octane alkylated gasoline by alkylation reaction of isobutane and butene.

[0060] During this reaction process, an ionic liquid is selected as the catalyst for the catalytic reaction.

[0061] Such as Figure 1As shown in the figure, the alkylation reaction device of the present invention includes: a reactor - 1 where the alkylation reaction occurs; three intensifying units are vertically arranged inside the reactor - 1 from bottom to top. Among them, the first intensifying unit - 15 is located at the bottom of the reactor - 1 and is directly connected to the gas storage tank - 10 through a pipeline. A gas pipeline control valve - 13 is arranged on the gas pipeline; a guiding port - 6 is arranged directly above the first intensifying unit - 15, and a baffle - 9 is arranged above the guiding port - 6. The second intensifying unit - 5 is arranged above the baffle - 9, and the second intensifying unit - 5 is connected to a mixing pipeline. The mixing pipeline is respectively connected to an ionic liquid storage tank - 7 and a liquid storage tank - 8 in a parallel manner. The third intensifying unit - 4 is arranged in the middle of the reactor, directly above the second intensifying unit - 5. A sensor - 2 is arranged above the third intensifying unit - 4. The sensor - 2 is closely attached to the inner wall of the reactor - 1. The controller - 3 can display the value detected by the sensor - 2 and control all the control valves in the reaction system. A main pipeline for discharging substances is arranged at the top of the reactor - 1. The main pipeline is connected to the first circulation pipeline and the second circulation pipeline in a parallel manner. A control valve a - 17 is arranged on the first circulation pipeline to control the opening and closing of the first circulation pipeline and the state of the internal circulation pipeline. The outlet of the first circulation pipeline is connected to the third intensifying unit - 4. A control valve b - 16 is arranged on the second circulation pipeline to control the opening and closing of the second circulation pipeline and the state of the internal circulation pipeline. A pipeline connection is made between the first circulation pipeline and the second circulation pipeline to form an internal circulation pipeline. A circulation pump - 18 is arranged on the internal circulation pipeline, and the control valve a - 17 and the control valve b - 16 are respectively arranged at the two connection points of the first circulation pipeline and the second circulation pipeline. The second circulation pipeline is connected to a phase separator - 20 through a gas - liquid separator - 19. At the same time, the gas - liquid separator - 19 is also provided with a pipeline connected to the gas storage tank - 10. The phase separator - 20 is connected to the ionic liquid storage tank - 7 through a pipeline, and at the same time, a pipeline outlet is also provided to be responsible for flowing the product out of the reaction system.

[0062] The practical application of the alkylation reactor in this embodiment includes the following processes:

[0063] The gas storage tank - 10 stores a mixture of butene and isobutane, where the molar ratio of isobutane to butene is 10:1. The liquid storage tank - 8 stores gasoline, and the ionic liquid storage tank - 7 stores an ionic liquid with strong acid function for catalysis. At the start of the reaction, the ionic liquid pipeline control valve - 11, the liquid pipeline control valve - 12, the gas pipeline control valve - 13, and the sensor - 2 are started by the controller, and the flow rate is adjusted through the control valves so that the reactants enter the reactor - 1 at a relatively reasonable flow rate. When the gas pipeline control valve - 13, the ionic liquid pipeline control valve - 11, and the liquid pipeline control valve - 12 are opened, the mixed gas of butene and isobutane enters the first intensification unit - 15 through the gas pipeline, and the two gases are fully mixed and broken in the first intensification unit - 15; gasoline enters the mixing pipeline through the liquid pipeline, and the ionic liquid enters the mixing pipeline through the ionic liquid pipeline. The gasoline and the ionic liquid are premixed once in the mixing pipeline, and then the premixed liquid enters the second intensification unit - 5 for breaking, so that the ionic liquid is fully dispersed in the gasoline. Subsequently, the mixed gas broken in the first intensification unit - 15 further collides and disperses through the guiding port - 6 and the baffle - 9, and then enters the second intensification unit - 5 to react with gasoline and ionic liquid to obtain high - octane alkylated gasoline.

[0064] The high - octane alkylated gasoline and a part of the unreacted butene and isobutane mixture enter the third intensification unit - 4 for breaking reaction. The sensor - 2 detects the state inside the reactor - 1 in real time and returns the state inside the reactor to the controller - 3. When the sensor - 2 detects that there are still some unreacted reactants, the controller that obtains the data at this time closes the control valve a - 17, the control valve b - 16, and opens the circulation pump - 18. At this time, the unreacted reactants first perform an internal circulation on the internal circulation pipeline under the action of the circulation pump - 18. Subsequently, the second circulation pipeline control valve b - 16 remains closed, and the control valve a - 17 is opened, so that the reactants enter the third intensification unit - 4 for reaction again. Then the sensor - 2 detects the reactants after the secondary reaction again and monitors the state inside the reactor - 1 in real time. At the same time, the controller - 3 closes the control valve a - 17, opens the control valve b - 16 and the circulation pump - 18, so that the mixture of high - octane alkylated gasoline, ionic liquid, and butene enters the gas - liquid separator - 19 through the second circulation pipeline, and the butene is separated from the reaction system. At this time, the controller - 3 opens the control valve d - 22, so that the separated butene returns to the gas storage tank - 10 through the pipeline and re - enters the reaction system for recycling. When the gas - liquid separation is completed, the controller - 3 opens the control valve c - 21, so that the liquid containing ionic liquid and high - octane alkylated gasoline enters the phase separator - 20 for separation. The separated ionic liquid re - enters the ionic liquid storage tank - 7, and the product high - octane alkylated gasoline flows out through the pipeline of the control valve e - 14.

[0065] The temperature in reactor 1 is controlled between 20°C and 30°C.

[0066] Example 2

[0067] Isobutane and butene are alkylated to produce high-octane alkylate gasoline.

[0068] It includes the following processes:

[0069] A mixture of butene and isobutane is stored in gas storage tank - 10, where the molar ratio of isobutane to butene is 10:1. Gasoline is stored in liquid storage tank - 8, and an ionic liquid with strong acid function for catalysis is stored in ionic liquid storage tank - 8. At the start of the reaction, the ionic liquid pipeline control valve - 11, liquid pipeline control valve - 12, gas pipeline control valve - 13 and sensor - 2 are started by the controller, and the flow rate is adjusted through the control valves so that the reactants enter reactor - 1 at a relatively reasonable flow rate. When gas pipeline control valve - 13, ionic liquid pipeline control valve - 11 and liquid pipeline control valve - 12 are opened, the mixed gas of butene and isobutane enters the first intensification unit - 15 through the gas pipeline, and the two gases are fully mixed and broken in the first intensification unit - 15; the gasoline liquid enters the mixing pipeline through the liquid pipeline, and the ionic liquid enters the mixing pipeline through the ionic liquid pipeline. The gasoline and the ionic liquid are premixed once in the mixing pipeline, and then the premixed liquid enters the second intensification unit - 5 for breaking, so that the ionic liquid is fully dispersed in the gasoline. Subsequently, the gas broken in the first intensification unit - 15 passes through the guiding port - 6 and the baffle - 9 for further collision and dispersion, and then enters the second intensification unit - 5 to react with the gasoline and the ionic liquid to obtain high-octane alkylate gasoline.

[0070] The high-octane alkylate gasoline and a part of the unreacted mixture of butene and isobutane enter the third intensification unit - 4 for breaking reaction. Sensor - 2 detects the state in reactor - 1 in real time and returns the state in the reactor to controller - 3. When it is detected in sensor - 2 that the reaction between isobutane and gasoline in reactor - 1 is completed, at this time controller - 3 closes control valve a - 17 and control valve b - 16, and the high-octane alkylate gasoline enters the separation device - 19 through control valve b - 16 for separation. After separation, controller - 3 opens control valve d - 22 to make the butene gas re-enter gas storage tank - 10 for reaction again. Controller - 3 opens control valve c - 21 and control valve e - 14 to make the liquid mixture remaining after gas-liquid separation enter the phase separator - 20 for separation. The high-octane alkylate gasoline obtained from the separation flows out through control valve e - 14, and the ionic liquid as the catalyst re-enters ionic liquid storage tank - 7 and then re-enters the reaction system.

[0071] The temperature inside the reactor 1 is controlled between 20°C and 30°C.

[0072] Example 3

[0073] Benzene reacts with ethylene to form ethylbenzene.

[0074] As Figure 2 shown, the alkylation reaction device of the present invention includes: the reactor - 101 where the alkylation reaction occurs; three strengthening units are vertically arranged inside the reactor - 101 from bottom to top. Among them, the first strengthening unit - 108 is located at the bottom of the reactor - 101 and is directly connected to the gas storage tank - 110 through a pipeline. A gas pipeline control valve - 109 is arranged on the gas pipeline; a guiding port - 107 is arranged directly above the first strengthening unit - 108, and a baffle - 106 is arranged above the guiding port - 107. The second strengthening unit - 105 is arranged above the baffle - 106. The second strengthening unit - 105 is connected to a mixing pipeline, and the mixing pipeline is respectively connected to the catalyst storage tank - 116 and the liquid storage tank - 117 in a parallel manner. The third strengthening unit - 104 is arranged in the middle of the reactor - 101, directly above the second strengthening unit - 105. A sensor - 103 is arranged above the third strengthening unit - 104. The sensor - 103 is closely attached to the inner wall of the reactor - 101. The controller - 102 can display the value detected by the sensor - 103 and control all the control valves in the reaction system. A main pipeline for discharging the substances participating in the reaction is arranged at the top of the reactor - 101. A heat exchanger - 111 is arranged on the main pipeline for heat exchange. The main pipeline is connected to the first circulation pipeline and the second circulation pipeline in a parallel manner. A control valve a - 113 is arranged on the first circulation pipeline for controlling the opening and closing of the first circulation pipeline and the state of the internal circulation pipeline. The outlet of the first circulation pipeline is connected to the third strengthening unit - 104. A control valve b - 114 is arranged on the second circulation pipeline for controlling the opening and closing of the second circulation pipeline and the state of the internal circulation pipeline. The first circulation pipeline and the second circulation pipeline are connected through a pipeline to form an internal circulation pipeline. A circulation pump - 112 is arranged on the internal circulation pipeline, and the control valve a - 113 and the control valve b - 114 are respectively arranged at the two connection points of the first circulation pipeline and the second circulation pipeline. The second circulation pipeline is respectively connected to the catalyst storage tank - 116 and the liquid storage tank - 117 through a distillation column - 115. The catalyst pipeline control valve - 118, the liquid pipeline control valve - 119, the control valve e - 120, the control valve f - 121, and the control valve g - 122 control the progress of the reaction.

[0075] The practical application of the alkylation reactor in this embodiment includes the following processes:

[0076] Ethylene is stored in the gas storage tank - 110, benzene is stored in the liquid storage tank - 117, and the catalyst is stored in the catalyst storage tank - 116. The catalyst catalyzes the occurrence of the reaction. At the start of the reaction, the catalyst pipeline control valve - 116, the liquid pipeline control valve - 119, the gas pipeline control valve - 109, and the sensor - 103 are started by the controller, and the valves are controlled to adjust the flow rate so that the reactants enter the reactor 101 at a relatively reasonable flow rate. When the gas pipeline control valve 109, the liquid pipeline control valve - 119, and the gas pipeline control valve - 109 are opened, the ethylene gas enters the intensification unit - 108 through the gas pipeline for fragmentation and dispersion. Benzene enters the mixing pipeline through the liquid pipeline, and the catalyst enters the mixing pipeline through the catalyst pipeline. Benzene and the catalyst are premixed once in the mixing pipeline, and then the premixed liquid enters the second intensification unit - 105 for fragmentation to fully disperse the catalyst in benzene. Subsequently, the gas fragmented in the first intensification unit - 108 is further collided and dispersed through the guiding port - 107 and the baffle - 106, and then enters the second intensification unit - 105 to react with benzene and the catalyst to obtain ethylbenzene.

[0077] Ethylbenzene and partially unreacted ethylene and gaseous benzene enter the third intensification unit - 104 for reaction. The sensor - 103 detects the state inside the reactor - 101 in real time and returns the state inside the reactor to the controller - 102. The reaction product is cooled by the heat exchanger - 111 on the main pipeline. At the same time, when the sensor - 103 detects that there are still some unreacted reactants, the controller that obtains the data closes the control valve a - 113, the control valve b - 114, and the circulation pump - 112. At this time, the unreacted reactants are first circulated once in the internal circulation pipeline under the action of the circulation pump - 112. Subsequently, the second circulation pipeline control valve b - 112 remains closed, and the control valve a - 114 is opened to make the reactants enter the third intensification unit - 104 for reaction again. Then the sensor - 103 detects the reactants after the secondary reaction again and monitors the state inside the reactor - 101 in real time. At the same time, the controller - 102 closes the control valve a - 113, opens the control valve b - 114, and the circulation pump - 112 to make the mixture of ethylbenzene, catalyst, and benzene enter the distillation column - 115 through the second circulation pipeline. Since benzene is in excess during the reaction of benzene and ethylene, there is no unreacted ethylene in the mixed liquid. Therefore, only the catalyst and benzene need to be separated from the reaction system. At this time, the controller - 102 opens the control valve f - 121 and the control valve e - 120 to make the distilled benzene return to the liquid storage tank - 117 through the pipeline and enter the reaction system again for recycling, and the catalyst returns to the catalyst storage tank - 116.

[0078] At this time, the reaction temperature in the reactor - 101 is controlled at 150°C - 160°C.

[0079] The reaction pressure is controlled at about 5 atmospheres.

[0080] Example 4

[0081] Benzene reacts with ethylene to form ethylbenzene.

[0082] Ethylene is stored in gas storage tank - 110, benzene is stored in liquid storage tank - 117, and the catalyst is stored in catalyst storage tank - 116. The catalyst catalyzes the reaction. At the start of the reaction, the catalyst pipeline control valve - 116, liquid pipeline control valve - 119, gas pipeline control valve - 109, and sensor - 103 are started by the controller, and the valves are controlled to adjust the flow rate so that the reactants enter the reactor 101 at a relatively reasonable flow rate. When the gas pipeline control valve 109, liquid pipeline control valve - 119, and gas pipeline control valve - 109 are opened, the ethylene gas enters the intensification unit - 108 through the gas pipeline for fragmentation and dispersion. Benzene enters the mixing pipeline through the liquid pipeline, and the catalyst enters the mixing pipeline through the catalyst pipeline. Benzene and the catalyst are premixed once in the mixing pipeline, and then the premixed liquid enters the second intensification unit - 105 for fragmentation to fully disperse the catalyst in benzene. Subsequently, the gas fragmented in the first intensification unit - 108 further collides and disperses through the guiding port - 107 and baffle - 106, and then enters the second intensification unit - 105 to react with benzene and the catalyst to obtain ethylbenzene.

[0083] Ethylbenzene, partially unreacted ethylene, and gaseous benzene enter the third intensification unit - 104 for reaction. The sensor - 103 detects the state inside the reactor - 101 in real - time and returns the state inside the reactor to the controller - 102. The reaction product is cooled by the heat exchanger - 111 on the main pipeline. At this time, the sensor - 103 detects that there is no unreacted benzene and ethylene in the reactor. The controller - 102 closes the control valve a - 113 and the circulation pump - 112 and opens the control valve b - 114. Since the reaction is complete, all the ethylene in the reaction device is consumed, and only benzene remains among the reactants. The product ethylbenzene and the catalyst enter the distillation column - 115 through the second circulation pipeline for distillation to obtain benzene, the catalyst, and the product ethylbenzene. At this time, the controller - 102 sequentially opens the control valve e - 120, control valve f - 121, and control valve g - 122 to return the catalyst to the catalyst storage tank - 116, return benzene to the liquid storage tank - 117, and let the product ethylbenzene flow out.

[0084] At this time, the reaction temperature in the reactor - 101 is controlled at 150 °C - 160 °C.

[0085] The reaction pressure is controlled at about 5 atmospheres.

[0086] Example 5

[0087] The specific implementation is the same as that of Example 1, except that the first circulation pipeline is not provided.

[0088] Example 6

[0089] The specific implementation is the same as that of the example, and the second circulation pipeline is not provided.

[0090] The specific reaction process is that the high-octane alkylated gasoline and other mixtures passing through the third intensification unit 4 directly enter the gas-liquid separator -19 and the phase separator -20 for separation.

[0091] Example 7

[0092] The specific implementation is the same as that of Example 1, except that the baffle and the guiding port are not provided.

[0093] Example 8

[0094] The specific implementation is the same as that of Example 1, except that the circulation pipeline is not provided.

[0095] Comparative Example 1

[0096] The reaction for preparing high-octane alkylated gasoline by the alkylation reaction of isobutane and butene.

[0097] The specific implementation is the same as that of Example 1, and the third intensification unit is not used.

[0098] Comparative Example 2

[0099] The reaction for preparing high-octane alkylated gasoline by the alkylation reaction of isobutane and butene.

[0100] The specific implementation is the same as that of Example 1, and the sensor and the controller are not provided.

[0101] Comparative Example 3

[0102] The reaction for preparing high-octane alkylated gasoline by the alkylation reaction of isobutane and butene.

[0103] Using hydrofluoric acid alkylation technology, the catalytic distillation technology completes the catalytic reaction and the rectification process in the same tower. The high-octane alkylated gasoline enters the acid settler for separation. The acid at the bottom of the settler is recycled. The hydrocarbon components at the top of the settler enter the fractionating tower to separate gases such as propane and n-butane. The product at the bottom of the tower is refined to obtain high-octane alkylated oil. The reaction temperature is 27°C - 43°C, and circulating water cooling is used.

[0104] Comparative Example 4

[0105] The reaction for preparing high-octane alkylated gasoline by the alkylation reaction of isobutane and butene.

[0106] The reaction is carried out using sulfuric acid alkylation technology.

[0107] The HQC ALKY technology adopts a horizontal alkylation reactor and a reaction effluent refrigeration process. The liquid-phase propane and butane in the reaction effluent are used to flash under reduced pressure in the reactor tube bundle to absorb the heat released by the alkylation reaction. The gas phase is recompressed, condensed by a compressor, and then recycled back to the reactor. The effluent refrigeration process can keep a high concentration of isobutane in the reactor. The recycled isobutane is mixed with butene hydrocarbons and enters the reactor. The acid-hydrocarbon is mechanically stirred by an impeller to form an emulsion, so that the hydrocarbons are evenly distributed in the acid, reducing the temperature gradient and inhibiting the occurrence of side reactions.

[0108] Comparative Example 5

[0109] The specific implementation is the same as that of Example 1, except that the third strengthening machine is set directly above the second strengthening unit, and the distance between the third strengthening unit and the second strengthening unit is equal to the distance between the first strengthening unit and the second strengthening unit.

[0110] Comparative Example 6

[0111] The specific implementation is the same as that of Example 1, except that the third strengthening unit is set directly above the second strengthening unit, and the third strengthening unit is close to the main pipeline.

[0112] Comparative Example 7

[0113] Ethylbenzene is produced by liquid-phase alkylation of benzene and ethylene.

[0114] The reaction is carried out by the AlCl3 liquid-phase method. The catalyst is dissolved in the benzene mixture. The inside of the reactor is dry benzene. The reaction process occurs in a homogeneous liquid-phase alkylation and transalkylation system. This process controls the catalyst addition amount within the solubility range of the liquid-phase aromatic hydrocarbons by adjusting the ethylene feed rate, so as to realize the reaction in a homogeneous liquid phase, and thus the alkylation reaction occurs.

[0115] Experimental Example 1

[0116] The reactions of the examples and comparative examples are carried out using different methods, and the conversion rates of the reaction raw materials participating in the reaction, the recovery rate of the catalyst, and the purity of the product are detected. The experimental results are shown in Table 1 and Table 2.

[0117] Table 1: Reaction results of isobutane and butene

[0118]

[0119] Table 2: Reaction results of liquid-phase alkylation of benzene and ethylene

[0120]

[0121] The following conclusions can be drawn from the above data:

[0122] It can be seen from the comparison between the examples and the comparative examples that when the device of the present invention is used, the raw material conversion rate, the catalyst recovery rate and the purity of the product can be significantly improved. At the same time, since the present invention uses ionic liquid as the catalyst, it can reduce the corrosion of strong acid to the reactor and extend the service life of the equipment.

[0123] The present invention sets up a three-stage enhanced reaction unit, and a baffle and a guiding port are arranged between the first enhanced reaction unit and the second enhanced reaction unit, so that all reactants participating in the reaction are fully dispersed and broken, which can multiply the mass transfer area and the total mass transfer rate between the reactants, thereby greatly increasing the reaction rate, effectively controlling side reactions and increasing the product yield, significantly reducing the energy consumption and material consumption in the reaction process, and improving the safety of the reaction section. At the same time, the setting of the three enhanced units and the setting of the two circulation pipelines enable the product to not require rectification separation, reducing the reaction energy consumption, recovering the ionic liquid, and being able to reuse the heat generated during the reaction process, reducing the reaction temperature and achieving the purpose of energy conservation.

[0124] When the enhanced unit is not set and the reaction is carried out using the traditional reaction method, the reactants and the ionic liquid cannot be well fused, and the mass transfer area is small, which makes the ionic liquid play its catalytic role well, thus reducing the reaction efficiency.

[0125] When the first circulation pipeline and the third enhanced unit are not set, the unreacted reactants cannot be subjected to a secondary reaction, thereby reducing the conversion rate of the reactants. When the second circulation pipeline and the phase separator are not set, the ionic liquid used as the catalyst cannot be well recovered and recycled, resulting in waste. The controller controls the flow rate or opening and closing of the control valve in the reaction device through the feedback of the sensor, achieving intelligent adjustment and real-time monitoring of the reaction process, ensuring the safety of the reaction and reducing unnecessary reaction processes that may produce by-products, reducing the content of by-products in the product and improving the purity of the product.

[0126] In the present invention, an internal circulation pipeline is also provided. The internal circulation pipeline can perform a primary mixing internal circulation on the unreacted reactants, enabling them to be pre-dispersed first, and then entering the third enhanced unit for a secondary reaction. The purpose of this setting is to ensure that when the reactants are not completely reacted, only one cycle is required to ensure that the reactants are completely reacted, improving the reaction efficiency of the reactants and saving energy and reducing energy consumption at the same time. During the reaction process of the reaction between benzene and ethylene, the reaction device used in the present invention can effectively reduce the reaction temperature and the temperature in the reactor, reduce energy consumption and ensure safety.

[0127] Finally, in the present invention, the position of the third intensifying unit is also defined. During the reaction, a large amount of gas will accumulate in the middle of the reactor. When the third intensifying unit is arranged at this position, it can ensure that the unreacted gas undergoes sufficient reaction, and at the same time, the sensor can cooperate with the third intensifying unit to better detect the situation inside the reactor. When the position of the third intensifying unit is too high, the sensor will detect the gas that has not passed through the third intensifying unit due to the irregular diffusion of the gas and give feedback, causing the controller to issue a wrong instruction, and finally resulting in an increase in by-products; while when the third intensifying unit is located at a lower position in the reactor, it may cause some gas to be inhaled by the second intensifying unit, leading to excessive reaction.

[0128] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those of ordinary skill in the art should understand that they can still modify the technical solutions described in the foregoing embodiments, or perform equivalent replacements on some or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. An alkylation reaction device, characterized in that: It comprises a reactor, wherein three strengthening units are vertically arranged inside the reactor; The first strengthening unit is arranged at the bottom of the reactor, the second strengthening unit is arranged directly above the first strengthening unit, and the third strengthening unit is arranged in the middle of the reactor; A sensor is also provided in the reactor, the sensor is closely attached to the inner wall of the reactor, and the sensor is located above the third strengthening unit; A main pipeline is arranged on the top of the reactor.

2. The alkylation reaction device according to claim 1, characterized in that: The main pipeline is connected in parallel with the first circulation pipeline and the second circulation pipeline; The first circulation pipeline is connected to the second circulation pipeline to form an internal circulation, and a circulation pump is arranged on the internal circulation pipeline; A control valve a and a control valve b are respectively provided at the connection between the first circulation pipeline and the second circulation pipeline; The outlet of the first circulation pipeline is connected to the third strengthening unit.

3. The alkylation reaction device according to claim 2, characterized in that: The second circulation pipeline is connected to the separation device; The separation device is connected to the storage tank.

4. The alkylation reaction device according to claim 1, characterized in that: A guide port is arranged above the first strengthening unit, and a baffle is arranged above the guide port.

5. The alkylation reaction device according to claim 3, characterized in that: The storage tanks include a catalyst storage tank, a gas storage tank and a liquid storage tank; The gas storage tank is directly connected to the first strengthening unit through a gas pipeline, and a gas pipeline control valve is provided on the gas pipeline; The catalyst storage tank provides catalyst through a catalyst pipeline control valve on the catalyst pipeline, and the liquid storage tank provides reaction liquid through a liquid pipeline control valve on the liquid pipeline. The catalyst pipeline and the liquid pipeline are connected in parallel to form a mixing pipeline, and the mixing pipeline is directly connected to the second enhancement unit.

6. The alkylation reaction device according to claim 1, characterized in that: A control valve is provided in the pipeline of the alkylation reaction device, and the reaction state is controlled by opening and closing the control valve and the flow rate.

7. The alkylation reaction device according to claim 1, characterized in that: The alkylation reaction device further comprises a controller, which can display the data transmitted from the sensor in real time and can control all control valves in the alkylation reaction device through the controller.

Images