Device and method for using self-rotating super / microgravity-microinterface synergistically enhanced carbon tetraalkylation reaction

Abstract

The present invention discloses a device for synergistically enhancing a C4 alkylation reaction by a self-rotating super / microgravity-microinterface. The device comprises: a heat exchanger, the number of which is ≥2; a series connection between the heat exchangers, i.e., a material outlet of the first heat exchanger is connected to a material inlet of the second heat exchanger; a super / microgravity-microinterface reactor; and a fluid conveyor. Furthermore, a method for using the device for synergistically enhancing a C4 alkylation reaction by a self-rotating super / microgravity-microinterface is disclosed. The present invention utilizes the self-rotating circular flow of the materials participating in the reaction within the reaction device to generate centrifugal force to overcome gravity and form a super / microgravity-microinterface field, thereby causing the heterogeneous reaction materials to form millimeter- or micrometer-sized droplets and bubbles, efficiently regulating the collective scale of the gas-liquid and gas-liquid-liquid interfaces from the milli-centimeter level to the micrometer level, and efficiently promoting interphase mixing and enhanced transfer processes of the heterogeneous reaction materials.

Description

Technical Field

[0001] The present invention relates to the technical field of chemical production equipment, and in particular to a device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction and a method for using the device. Background Art

[0002] Sulfuric acid-catalyzed C4 alkylation is a large-scale industrial process currently used and is relatively safe, stable, and reliable. During the alkylation process, RON is the most important evaluation criterion for the alkylate oil product and is highly demanding. The sulfuric acid-catalyzed C4 alkylation reaction is a rapid and complex liquid-liquid two-phase process. Improving the mixing state and mass transfer between the acid and hydrocarbon phases is crucial for improving the quality of the alkylate oil product. High-gravity technology excels in enhancing micro-mixing and mass transfer, and has become a key technology for intensifying the C4 alkylation process.

[0003] In the prior art, CN114085682 A discloses a sulfuric acid alkylation reaction method and apparatus, as well as a heat extraction method for the sulfuric acid alkylation reaction. The sulfuric acid alkylation reaction method, apparatus, and heat extraction method provided by this technology significantly reduce the total energy consumption of the alkylation reaction apparatus and reduce equipment investment. CN209128343 U discloses an experimental apparatus for C4 alkylation. This utility model experimental apparatus has precise metering, safety, and reliability. CN106542951 A discloses a method for reducing the amount of sulfuric acid used in the alkylation reaction using a high-efficiency adsorbent. This technology is simple in process, easy to operate, and easy to implement. It also requires little equipment investment, has low overall costs, and is free of secondary pollution, resulting in significant economic and social benefits. CN112662426 A discloses a liquid acid alkylation reaction method and apparatus. This invention utilizes a concentrated sulfuric acid catalyst system formed from fuming sulfuric acid, which improves the selectivity and octane number of the alkylation product and reduces the production of non-ideal products. CN112473723A discloses a high-acidity catalyst, its preparation method, and a C4 alkylation reaction method. The disclosed catalyst significantly increases the acidity, exhibits excellent reactivity, high selectivity, and a long lifespan. Furthermore, the catalyst preparation process is simple, making it suitable for large-scale industrial production. CN107974280 A discloses a liquid acid alkylation reaction method, which provides high selectivity for liquid acid alkylation reactions.

[0004] The above invention applications all utilize mechanical equipment and precision instruments to generate supergravity, micro-interface, ultrasonic waves, microwaves and turntable effects to enhance the chemical transfer process, resulting in high energy consumption, equipment investment and operational difficulty. Summary of the Invention

[0005] To solve the above technical problems, the present invention provides a device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction and its use method, which utilizes the centrifugal force generated by the rotational flow of the reaction materials themselves to overcome the gravitational field and form a super / microgravity field, thereby achieving the goals of convenient operation, energy saving and consumption reduction, and reduced equipment investment costs.

[0006] To achieve the above objectives, the present invention provides the following technical solutions:

[0007] A device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction, the device comprising:

[0008] A heat exchanger having a material inlet and a material outlet at its upper and lower ends, respectively, and a heat exchange fluid inlet and a heat exchange fluid outlet at its side wall; the number of the heat exchangers is ≥ 2, and the heat exchangers are connected in series, that is, the material outlet of the first heat exchanger is connected to the material inlet of the second heat exchanger, and so on;

[0009] A super / microgravity-microinterface reactor, disposed within the heat exchanger, comprising a fluid central tube and a fluid distributor, wherein the fluid central tube is a cylindrical tube with an open upper end, the upper end of the fluid central tube being connected to the material inlet; at least one fluid distributor being disposed axially of the fluid central tube, the fluid distributor comprising at least four arc bend groups, each arc bend group comprising at least one arc bend, the arc bends being radially distributed; when the number of arc bends in each arc bend group is ≥2, the arc diameters of the arc bends increase sequentially from the inside to the outside; a nozzle being disposed at the outer end of the arc bend, the inner end of the nozzle being connected to the fluid central tube; and

[0010] A fluid conveyor, wherein the material inlet is communicated with the fluid conveyor.

[0011] Furthermore, the heat exchanger is a shell and tube heat exchanger or a jacketed heat exchanger.

[0012] Furthermore, 2 to 40 fluid distributors are arranged in the axial direction of the fluid central tube, and the interval between each fluid distributor is 50 mm to 800 mm.

[0013] Furthermore, the heat exchanger has a diameter of 2000 mm to 10000 mm and a height of 4000 mm to 20000 mm.

[0014] Furthermore, in each arc bend pipe group, the number of the arc bend pipes is 1 to 10, and the arc diameter of the arc bend pipe is 100 mm to 9000 mm.

[0015] Furthermore, the nozzle diameter is 1 mm to 10 mm, and the arc elbow diameter is 3 mm to 20 mm.

[0016] A method for using the above-mentioned device for synergistically enhancing a C4 alkylation reaction under a rotating super / microgravity-microinterface environment comprises the following steps:

[0017] (1) The heat exchange fluid inlet and the heat exchange fluid outlet are connected to the device for providing cold fluid for heat exchange; the fluid conveyor is connected to each device for providing materials, and is used to convey the materials C4 alkane, sulfuric acid or ionic liquid, and C4 olefin to the material inlet respectively, and enter the fluid center tube of the super / microgravity-micro interface reactor through the material inlet, that is, after the C4 alkane, sulfuric acid or ionic liquid, and C4 olefin enter the first heat exchanger for reaction, the resulting mixture is discharged through the material outlet of the first heat exchanger and then enters the second heat exchanger from the material inlet of the second heat exchanger. At the same time, C4 alkane and C4 olefin are supplemented at the material inlet of the second heat exchanger. The material flow rate of the material conveyed by the fluid conveyor is determined by the size of the β value, and the specific calculation formula is as follows:

[0018] Centrifugal acceleration is G = Rω 2 (1)

[0019] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0020] Hypergravity / microgravity factors

[0021] Where: G-centrifugal acceleration, m / s 2 ;

[0022] R-circular motion radius, that is, the arc radius of the arc bend, m;

[0023] g-Earth's gravitational acceleration, m / s 2 ;

[0024] ω-angular velocity of circular motion, i.e., the angular velocity of the material in the super / microgravity-microinterface reactor, 1 / s;

[0025] β-hyper / microgravity factor;

[0026] N-circular motion speed, r / min;

[0027] π - pi;

[0028] V-circular motion linear velocity, i.e., the flow rate of the material in the super / microgravity-microinterface reactor, m / s;

[0029] Wherein, R is a known value, and β takes a specific value so that the material is in a microgravity or supergravity state in the super / microgravity-microinterface reactor;

[0030] (2) After C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins enter the fluid center tube, they are sprayed into the heat exchanger through the arc bend and nozzle to achieve mixing and reaction. The mixture obtained after the reaction in the first heat exchanger enters the second heat exchanger from the material outlet. At the same time, C4 alkanes and C4 olefins are added to the material inlet of the second heat exchanger. The flow rates of C4 alkanes and C4 olefins are also controlled to comply with the above formula.

[0031] Among them, when the centrifugal acceleration G is 1 to 50 times the earth's gravitational acceleration g, that is, β = 1 to 50, a microgravity field effect is generated; when the centrifugal acceleration G is greater than 50 times the earth's gravitational acceleration g, that is, β>50, a supergravity field effect is generated, thereby causing the heterogeneous reaction materials to form millimeter-level or micron-level small droplets and small bubbles, effectively promoting the mixing and enhanced transfer process between the heterogeneous reaction materials. The β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material.

[0032] Compared with the prior art, the present invention has the following beneficial effects:

[0033] The present invention utilizes the self-rotating circular flow of materials participating in the reaction within a reaction device to generate centrifugal force, thereby overcoming gravity to form a super / microgravity-microinterface field, thereby causing the heterogeneous reaction materials to form millimeter-scale or micron-scale droplets and small bubbles, and efficiently controlling the collective scale of the gas-liquid and gas-liquid-liquid interfaces from the milli-centimeter level to the micron level, thereby efficiently promoting interphase mixing and enhancing the transfer process of the heterogeneous reaction materials. Furthermore, the reaction device of the present invention does not require the use of special mechanical equipment to drive the reaction materials to rotate at high speed to generate centrifugal force. Due to the self-rotating circular flow of the reaction materials in the reaction device of the present invention, the super / microgravity-microinterface is generated, thereby enhancing the transfer process of the reaction system. The device has a simple structure, is easy to manufacture, convenient to install and maintain, has good sealing performance, and is simple to operate, thereby achieving high-efficiency, low-energy consumption, low-pollution, and low-investment industrial production. BRIEF DESCRIPTION OF THE DRAWINGS

[0034] Figure 1 It is a schematic diagram of the device for the self-rotating super / microgravity-microinterface synergistic enhancement of the carbon tetraalkylation unit reaction of the present invention.

[0035] Figure 2 This is a top view of the super / microgravity-micro interface reactor.

[0036] Figure 3 are heat exchangers, where (a) is a shell and tube heat exchanger and (b) is a jacketed heat exchanger.

[0037] Figure 4This is a schematic diagram of two heat exchangers connected in series in the device for the self-rotating super / microgravity-microinterface synergistic enhancement of carbon tetraalkylation reaction of the present invention.

[0038] Figure 5 This is a schematic diagram of three heat exchangers connected in series in the device for the self-rotating super / microgravity-microinterface synergistic enhancement of C4 alkylation reaction of the present invention.

[0039] Figure 6 This is a three-dimensional diagram of the super / microgravity-micro interface reactor.

[0040] Among them, 1-heat exchanger, 2-fluid center pipe, 3-fluid distributor, 4-fluid conveyor; 11-first heat exchanger, 12-second heat exchanger, 13-third heat exchanger, 101-material inlet, 102-material outlet, 103-heat exchange fluid inlet, 104-heat exchange fluid outlet, 301-arc elbow, 302-nozzle. DETAILED DESCRIPTION

[0041] The following is a detailed description of the specific embodiments in conjunction with the accompanying drawings, but it should be understood that the scope of protection of the present invention is not limited by the specific embodiments. Unless otherwise specified, the raw materials and reagents used in the examples are all commercially available.

[0042] Unless expressly stated otherwise, throughout the specification and claims, the term "comprise" or variations such as "include" or "comprising", etc., will be understood to include the stated elements or components but not to exclude other elements or other components.

[0043] Example 1

[0044] Figure 1 The schematic diagram of the structure of a device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction of the present invention is shown. The device for the reaction includes:

[0045] Heat exchanger 1 has a material inlet 101 at its upper end and a material outlet 102 at its lower end. A heat exchange fluid inlet 103 and a heat exchange fluid outlet 104 are provided on the side wall of heat exchanger 1. The number of heat exchangers 1 is ≥ 2. The heat exchangers are connected in series, i.e., the material outlet 102 of the first heat exchanger 11 is connected to the material inlet 101 of the second heat exchanger 12, and so on. The reaction proceeds in the heat exchanger 1, and the reaction process releases heat. A cold fluid enters and exits the heat exchanger 1 to achieve the purpose of controlling the reaction temperature.

[0046] Super / microgravity-microinterface reactor ( Figure 2 and Figure 6), which is arranged in the heat exchanger 1, the super / microgravity-micro interface reactor includes a fluid center tube 2 and a fluid distributor 3, the fluid center tube 2 is a cylindrical tube with an upper end open, and the upper end of the fluid center tube 2 is connected to the material inlet 101; at least one fluid distributor 3 is arranged axially of the fluid center tube 2, and the fluid distributor 3 includes at least four arc bend groups, each arc bend group includes at least one arc bend 301, and the arc bends 301 are radially distributed; when the number of arc bends 301 in each arc bend group is ≥2, the arc diameter of the arc bend 301 is from the inside to the outside The length of the circular arc bend 301 is increased successively, so that when the materials are ejected from the nozzles 302 of the arc bends 301 of different lengths, the reaction materials in different areas can be stirred to make the reaction more complete; the outer end of the circular arc bend 301 is provided with a nozzle 302, and the inner end of the circular arc bend 301 is connected to the fluid center tube 2; the materials are mixed and reacted by passing through the super / microgravity-micro interface reactor, that is, the materials enter the fluid center tube 2 to complete the primary mixing (chemical reaction also occurs between the materials during the mixing period), and then are ejected into the heat exchanger 1 through the fluid distributor 3 to achieve secondary mixing and reaction;

[0047] and a fluid conveyor 4, wherein the material inlet 101 is in communication with the fluid conveyor 4 and is used for conveying the materials into the super / microgravity-microinterface reactor;

[0048] refer to Figure 1 and Figure 5 When the number of heat exchangers is 3, the material outlet 102 of the first heat exchanger 11 is connected to the material inlet 101 of the second heat exchanger 12, and the material outlet 102 of the second heat exchanger 12 is connected to the material inlet 101 of the third heat exchanger 13.

[0049] refer to Figure 1 and Figure 3 , the heat exchanger 1 is a shell and tube heat exchanger or a jacketed heat exchanger.

[0050] refer to Figure 1 and Figure 2 , 2 to 40 fluid distributors 3 are arranged axially in the fluid center tube 2, and the interval between each fluid distributor 3 is 50 mm to 800 mm. The number of fluid distributors 3 depends on the size of the heat exchanger 1. The larger the heat exchanger 1 is, the more fluid distributors 3 there are. The more fluid distributors 3 there are, the more uniform the mixing is and the more sufficient the stirring is.

[0051] refer to Figure 1 and Figure 3 The heat exchanger 1 has a diameter of 2000mm to 10000mm and a height of 4000mm to 20000mm.

[0052] refer to Figure 2In each arc bend pipe group, the number of the arc bend pipes 301 is 1 to 10, and the arc diameter of the arc bend pipe 301 is 100 mm to 9000 mm.

[0053] Continue to refer Figure 2 The diameter of the nozzle 302 is 1 mm to 10 mm, and the diameter of the arc elbow 301 is 3 mm to 20 mm.

[0054] Example 2

[0055] The method for using the apparatus for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction in Example 1 is as follows:

[0056] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device for providing cold fluid for heat exchange. The heat exchanger 1 has a diameter of 2000 mm and a height of 4000 mm. There are two heat exchangers 1 connected in series (such as Figure 4 ), the materials C4 alkane, sulfuric acid or ionic liquid, and C4 olefin are respectively transported to the material inlet 101 at a certain speed through the fluid conveyor 4, and enter the fluid central tube 2 through the material inlet 101. There are 4 arc bend groups in each heat exchanger 1, and each arc bend group has three arc bends 301. The arc diameter of the first arc bend is 200 mm, the arc diameter of the second arc bend is 900 mm, and the arc diameter of the third arc bend is 1500 mm. The diameter of the nozzle 302 is 3 mm, the diameter of the arc bend 301 is 9 mm, and there are 8 fluid distributors 3; the C4 alkane, sulfuric acid or ionic liquid, and C4 olefin enter the first heat exchanger 11 for reaction, and the mixture obtained after the reaction enters the second heat exchanger 12 through the material outlet 102 of the first heat exchanger 11. Among them, the material flow rate V of the material transported by the fluid conveyor 4 is determined by the size of the β value, and the material flow rate is controlled to be 14.9 m / s. The specific calculation formula is as follows:

[0057] Centrifugal acceleration is G = Rω 2 (1)

[0058] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0059] Hypergravity / microgravity factors

[0060] Where: G—centrifugal acceleration, m / s 2 ; R—circular motion radius, m; g—earth gravity acceleration, m / s 2 ;ω—angular velocity of circular motion, 1 / s;β—super / microgravity factor;N—rotational speed of circular motion, r / min;π—pi;V—linear velocity of circular motion, m / s;

[0061] Specifically, after each material enters the fluid center tube 2, it is in a super / micro-gravity state, and β≥30. At this time, G≥294.3m / s 2 Because there are three arc bends 301, each with a different arc radius, in order to ensure that the β value meets the above requirements, the arc radius of the largest arc bend is used to calculate V, that is, R = 0.75m, then V = 14.9m / s; because the arc radius of the arc bends in the super / microgravity-microinterface reactor is different, the material will be stirred at different positions in the heat exchanger 1 when it is ejected, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0062] (2) The C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins flowing in from the material inlet 101 are mixed once in the fluid center tube 2. Since the lower end of the fluid center tube 2 is closed, the materials can only enter the arc bend 301 from the fluid center tube 2 and be ejected through the nozzle 302. Due to the speed given by the fluid conveyor 4, the ejected materials generate centrifugal force, overcome gravity to form a super / microgravity-micro interface field, achieve the purpose of strengthening the transfer process of the reaction system, and carry out a mixing reaction in this process. The mixture obtained after the reaction in the first heat exchanger 11 enters the second heat exchanger 12 from the material outlet 102 due to the pressure difference. At the same time, the material inlet 101 of the second heat exchanger 12 is supplemented. Add C4 alkanes and C4 olefins (the corresponding material speed during addition must also satisfy the above equation), sulfuric acid or ionic liquid as a catalyst, no further replenishment is required. If the number of heat exchangers is greater than 3, the catalyst can be replenished as appropriate. The added C4 alkanes and C4 olefins and the reacted mixture from the first heat exchanger 11 continue to mix and react in the second heat exchanger 12, and the product obtained after the reaction is discharged from the material outlet 102; during the reaction, a cold fluid enters from the heat exchange fluid inlet 103, completes heat exchange with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104; the series connection method can avoid the back-mixing phenomenon in the heat exchanger 1, improve the driving force of the reaction process, and extend the reaction time.

[0063] Example 3

[0064] The method for using the apparatus for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction in Example 1 is as follows:

[0065] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device for providing cold fluid for heat exchange. The heat exchanger 1 has a diameter of 5000 mm and a height of 10000 mm. There are two heat exchangers 1 connected in series (such as Figure 4), the materials C4 alkane, sulfuric acid or ionic liquid, and C4 olefin are respectively transported to the material inlet 101 at a certain speed through the fluid conveyor 4, and enter the fluid center tube 2 through the material inlet 101. There are 4 arc bend groups in each heat exchanger 1, and each arc bend group has five arc bends 301. The arc diameter of the first one is 300mm, the arc diameter of the second one is 1000mm, the arc diameter of the third one is 2000mm, the arc diameter of the fourth one is 3000mm, and the arc diameter of the fifth one is 1000mm. The diameter of the arc is 4000 mm, the diameter of the nozzle 302 is 10 mm, the diameter of the arc elbow 301 is 20 mm, and there are 20 fluid distributors 3. C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins enter the first heat exchanger 11 for reaction. The resulting mixture enters the second heat exchanger 12 through the material outlet 102 of the first heat exchanger 11. The material flow rate V of the material transported by the fluid conveyor 4 is determined by the β value, and the material flow rate is controlled to be 4.44 m / s. The specific calculation formula is as follows:

[0066] Centrifugal acceleration is G = Rω 2 (1)

[0067] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0068] Hypergravity / microgravity factors

[0069] Where: G-centrifugal acceleration, m / s 2 ; R-circular motion radius, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, 1 / s;β-super / microgravity factor;N-rotational speed of circular motion, r / min;π-circular ratio;V-linear velocity of circular motion, m / s;

[0070] Specifically, after each material enters the fluid center tube 2, it is in a slightly heavy state, and β≥1. At this time, G≥9.81m / s 2 Because there are five arc bends 301, each with a different arc radius, in order to ensure that the β value meets the above requirements, the arc radius of the largest arc bend is used to calculate V, that is, R = 2m, then V = 4.44m / s; because the arc radius of the arc bends in the super / microgravity-microinterface reactor is different, the material will be stirred at different positions in the heat exchanger 1 when it is ejected, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0071] (2) The C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins flowing in from the material inlet 101 are mixed once in the fluid center tube 2. Since the lower end of the fluid center tube 2 is closed, the materials can only enter the arc bend 301 from the fluid center tube 2 and be ejected through the nozzle 302. Due to the speed given by the fluid conveyor 4, the ejected materials generate centrifugal force, overcome gravity to form a microgravity-microinterface field, and achieve the purpose of strengthening the transfer process of the reaction system. In this process, a fully mixed reaction is carried out. After the reaction in the first heat exchanger 11, the mixture obtained enters the second heat exchanger 12 from the material outlet 102 due to the pressure difference. At the same time, the material inlet 101 of the second heat exchanger 12 is supplemented. Add C4 alkanes and C4 olefins (the corresponding material speed during addition must also satisfy the above equation), sulfuric acid or ionic liquid as a catalyst, no further replenishment is required. If the number of heat exchangers is greater than 3, the catalyst can be replenished as appropriate. The added C4 alkanes and C4 olefins and the reacted mixture from the first heat exchanger 11 continue to mix and react in the second heat exchanger 12, and the product obtained after the reaction is discharged from the material outlet 102; during the reaction, a cold fluid enters from the heat exchange fluid inlet 103, completes heat exchange with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104; the series connection method can avoid the back-mixing phenomenon in the heat exchanger 1, improve the driving force of the reaction process, and extend the reaction time.

[0072] Example 4

[0073] The method for using the apparatus for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction in Example 1 is as follows:

[0074] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device for providing cold fluid for heat exchange. The heat exchanger 1 has a diameter of 8000 mm and a height of 16000 mm. There are three heat exchangers 1 connected in series (such as Figure 5), the materials C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins are respectively transported to the material inlet 101 at a certain speed through the fluid conveyor 4, and enter the fluid center tube 2 through the material inlet 101. There are 4 arc bend groups in each heat exchanger 1, and each arc bend group has seven arc bends 301. The arc diameter of the first arc bend is 500 mm, the arc diameter of the second arc bend is 1000 mm, the arc diameter of the third arc bend is 2000 mm, the arc diameter of the fourth arc bend is 3000 mm, the arc diameter of the fifth arc bend is 4000 mm, the arc diameter of the sixth arc bend is 5000 mm, and the arc diameter of the seventh arc bend is 5000 mm. The arc diameter is 7500mm, the diameter of the nozzle 302 is 8mm, the diameter of the arc elbow 301 is 15mm, and there are 30 fluid distributors 3; after the carbon four alkanes, sulfuric acid or ionic liquids, and carbon four olefins enter the first heat exchanger 11 for reaction, the mixture obtained after the reaction enters the second heat exchanger 12 through the material outlet of the first heat exchanger 11, and the mixture obtained after the reaction of the second heat exchanger 12 is discharged through the material outlet 102 of the second heat exchanger 12 and enters the third heat exchanger 13 from the material inlet 101 of the third heat exchanger 13, wherein the material transported by the fluid conveyor 4 is determined by the size of the β value. The material flow rate V is controlled to be 38.48m / s. The specific calculation formula is as follows:

[0075] Centrifugal acceleration is G = Rω 2 (1)

[0076] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0077] Hypergravity / microgravity factors

[0078] Where: G—centrifugal acceleration, m / s 2 ; R—circular motion radius, m; g—earth gravity acceleration, m / s 2 ;ω—angular velocity of circular motion, 1 / s;β—super / microgravity factor;N—rotational speed of circular motion, r / min;π—pi;V—linear velocity of circular motion, m / s;

[0079] Specifically, after each material enters the fluid center tube 2, it is in a super / micro-gravity state, and β≥40. At this time, G≥392.4m / s 2Because there are seven arc bends 301, each with a different arc radius, in order to ensure that the β value meets the above requirements, the arc radius of the largest arc bend is used to calculate V, that is, R = 3.75m, then V = 38.48m / s; because the arc radius of the arc bends in the super / microgravity-microinterface reactor is different, the material will be stirred at different positions in the heat exchanger 1 when it is ejected, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0080] (2) The C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins flowing in from the material inlet 101 are mixed once in the fluid central tube 2. Since the lower end of the fluid central tube 2 is closed, the materials can only enter the arc bend 301 from the fluid central tube 2 and be ejected through the nozzle 302. Due to the speed imparted by the fluid conveyor 4, the ejected materials generate centrifugal force, overcome gravity to form a super / microgravity-micro interface field, thereby achieving the transmission process of the enhanced reaction system, and mixing and reaction are carried out in this process. The mixture obtained after the reaction in the first heat exchanger 11 enters the second heat exchanger 12 from the material outlet 101. At the same time, C4 alkanes and C4 olefins are supplemented at the material inlet 101 of the second heat exchanger 12 (the corresponding material speed during addition must also satisfy the above equation). The mixture obtained after the reaction in the second heat exchanger 11 enters the material outlet 101. 101 enters the third heat exchanger 13, and C4 alkanes and C4 olefins are supplemented at the material inlet 101 of the third heat exchanger 13 (the corresponding material speed during addition must also satisfy the above equation). Sulfuric acid or ionic liquid is used as a catalyst and does not need to be supplemented. If the number of heat exchangers 1 is greater than 3, the catalyst can be supplemented as appropriate. The supplemented C4 alkanes and C4 olefins and the reacted mixture from the first heat exchanger 11 / the second heat exchanger 12 continue to mix and react in the second heat exchanger 12 / the third heat exchanger 13, and the product obtained after the reaction is discharged from the material outlet 102; during the reaction, a cold fluid enters from the heat exchange fluid inlet 103, completes heat exchange with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104; the series connection method can avoid the back-mixing phenomenon in the heat exchanger 1, improve the driving force of the reaction process, and extend the reaction time.

[0081] Example 5

[0082] The method for using the apparatus for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction in Example 1 is as follows:

[0083] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device for providing cold fluid for heat exchange. The heat exchanger 1 has a diameter of 5000 mm and a height of 12000 mm. There are two heat exchangers 1 connected in series (such as Figure 4), the materials C4 alkane, sulfuric acid or ionic liquid, and C4 olefin are respectively transported to the material inlet 101 at a certain speed through the fluid conveyor 4, and enter the fluid center pipe 2 through the material inlet 101. There are 4 arc bend groups in each heat exchanger 1, and each arc bend group has four arc bends 301. The arc diameter of the first arc bend is 200 mm, the arc diameter of the second arc bend is 1000 mm, the arc diameter of the third arc bend is 2500 mm, and the arc diameter of the fourth arc bend is 2000 mm. The arc diameter is 4000 mm, the diameter of the nozzle 302 is 6 mm, the diameter of the arc elbow 301 is 12 mm, and there are 25 fluid distributors 3; C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins enter the first heat exchanger 11 for reaction, and the resulting mixture enters the second heat exchanger 12 through the material outlet 102 of the first heat exchanger 11. The material flow rate V of the material transported by the fluid conveyor 4 is determined by the β value, and the material flow rate is controlled to be 34.41 m / s. The specific calculation formula is as follows:

[0084] Centrifugal acceleration is G = Rω 2 (1)

[0085] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0086] Hypergravity / microgravity factors

[0087] Where: G-centrifugal acceleration, m / s 2 ; R-circular motion radius, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, 1 / s;β-super / microgravity factor;N-rotational speed of circular motion, r / min;π-circular ratio;V-linear velocity of circular motion, m / s;

[0088] Specifically, each material is in an overweight state after entering the fluid center pipe 2, and β is set to be ≥ 60. At this time, G is ≥ 588.6 m / s 2 Because there are four arc bends 301, each with a different arc radius, in order to ensure that the β value meets the above requirements, the arc radius of the largest arc bend is used to calculate V, that is, R = 2m, then V = 34.41m / s; because the arc radius of the arc bends in the super / microgravity-microinterface reactor is different, the material will be stirred at different positions in the heat exchanger 1 when it is ejected, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0089] (2) The C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins flowing in from the material inlet 101 are mixed once in the fluid central tube 2. Since the lower end of the fluid central tube 2 is closed, the materials can only enter the arc bend 301 from the fluid central tube 2 and be ejected through the nozzle 302. Due to the speed given by the fluid conveyor 4, the ejected materials generate centrifugal force, overcome gravity to form a supergravity-micro interface field, and achieve the purpose of strengthening the transfer process of the reaction system. In this process, a mixing reaction is carried out. After the reaction in the first heat exchanger 11, the mixture obtained enters the second heat exchanger 12 from the material outlet 102 due to the pressure difference. At the same time, the material inlet 101 of the second heat exchanger 12 is supplemented. C4 alkanes and C4 olefins (the corresponding material speeds when added must also satisfy the above equation), sulfuric acid or ionic liquids serve as catalysts and do not need to be replenished. If the number of heat exchangers is greater than 3, catalysts can be replenished as appropriate. The added C4 alkanes and C4 olefins and the reacted mixture from the first heat exchanger 11 continue to mix and react in the second heat exchanger 12, and the products obtained after the reaction are discharged from the material outlet 102. During the reaction, a cold fluid enters from the heat exchange fluid inlet 103, completes heat exchange with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104. The series connection can avoid back-mixing in the heat exchanger 1, increase the driving force of the reaction process, and extend the reaction time.

[0090] The foregoing descriptions of specific exemplary embodiments of the present invention are for purposes of illustration and description. These descriptions are not intended to limit the invention to the precise forms disclosed, and it is apparent that many variations and modifications are possible in light of the foregoing teachings. The exemplary embodiments have been selected and described for the purpose of explaining the specific principles of the invention and their practical application, thereby enabling those skilled in the art to realize and utilize a variety of exemplary embodiments of the invention and various options and modifications. The scope of the invention is intended to be defined by the claims and their equivalents.

Claims

1. A device for synergistically enhancing C4 alkylation reaction by self-rotating super / microgravity-microinterface, characterized by: The device of the reaction comprises: A heat exchanger having a material inlet and a material outlet at its upper and lower ends, respectively, and a heat exchange fluid inlet and a heat exchange fluid outlet at its side wall; the number of the heat exchangers is ≥ 2, and the heat exchangers are connected in series, that is, the material outlet of the first heat exchanger is connected to the material inlet of the second heat exchanger, and so on; A super / microgravity-microinterface reactor, disposed within the heat exchanger, comprising a fluid central tube and a fluid distributor, wherein the fluid central tube is a cylindrical tube with an open upper end, the upper end of the fluid central tube being connected to the material inlet; at least one fluid distributor being disposed axially of the fluid central tube, the fluid distributor comprising at least four arc bend tube groups, each arc bend tube group comprising at least two arc bend tubes, the arc bend tubes being radially distributed, the arc diameters of the arc bend tubes increasing sequentially from the inside to the outside; a nozzle being disposed at the outer end of the arc bend tube, the inner end of which being connected to the fluid central tube; and A fluid conveyor, wherein the material inlet is communicated with the fluid conveyor.

2. The device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction according to claim 1, characterized in that: The heat exchanger is a shell and tube heat exchanger or a jacketed heat exchanger.

3. The device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction according to claim 1, characterized in that: The fluid central tube is provided with 2 to 40 fluid distributors in the axial direction, and the interval between each fluid distributor is 50 mm to 800 mm.

4. The device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction according to claim 1, characterized in that: The heat exchanger has a diameter of 2000 mm to 10000 mm and a height of 4000 mm to 20000 mm.

5. The device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction according to claim 1, characterized in that: In each arc bend pipe group, the number of the arc bend pipes is 2 to 10, and the arc diameter of the arc bend pipe is 100 mm to 9000 mm.

6. The device for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction according to claim 1, characterized in that: The nozzle diameter is 1 mm to 10 mm, and the arc elbow diameter is 3 mm to 20 mm.

7. A method for using the apparatus for self-rotating super / microgravity-microinterface synergistically enhancing C4 alkylation reaction as claimed in claim 1, characterized in that: The following steps are involved: (1) The heat exchange fluid inlet and the heat exchange fluid outlet are connected to a device for providing a cold fluid, and the materials C4 alkanes, sulfuric acid or ionic liquid, and C4 olefins are transported to the fluid center tube through a fluid conveyor. That is, the C4 alkanes, sulfuric acid or ionic liquid, and C4 olefins enter the first heat exchanger for reaction, and the resulting mixture enters the second heat exchanger through the material outlet of the first heat exchanger. At the same time, C4 alkanes and C4 olefins are added to the material inlet of the second heat exchanger; (2) After C4 alkanes, sulfuric acid or ionic liquids, and C4 olefins enter the fluid center tube, they are sprayed into the heat exchanger through the arc bend and nozzle to achieve mixing and reaction.

Images