A self-rotating bed ultra / micro-gravity - micro-interface reaction device and its usage method

Abstract

The present invention discloses a self-rotating bed super / microgravity-microinterface reaction device and a method for using the same. The reaction device comprises: a cylindrical heat exchanger, wherein the left and right ends thereof are respectively provided with a first material inlet and a material outlet, a heat exchange fluid inlet and a heat exchange fluid outlet are provided on the side wall thereof, and at least two second material inlets are provided on the side wall thereof; a coil reactor, wherein the coil comprises a coil, the coil is in a cylindrical spiral shape, and the coil is arranged in the cylindrical heat exchanger in a manner distributed along the left and right directions with the axis; the left end of the coil is connected to the first material inlet, and the right end of the coil is connected to the material outlet; the coil is provided with two material ports, each of which is connected to a second material inlet; and a fluid conveyor, wherein the first material inlet and the two second material inlets are each connected to a fluid conveyor; and a method for using the reaction device. The reaction device of the present invention has a simple structure and reliable operation, and can achieve the industrial production goals of high efficiency, low energy consumption and low investment.

Description

Technical Field

[0001] The present invention relates to the field of chemical technology, and in particular to a self-rotating bed super / microgravity-microinterface reaction device and a use method thereof. Background Art

[0002] Reaction units are core equipment in chemical production processes. Because chemical production processes such as redox, catalytic hydrogenation, esterification, condensation, alkylation, sulfonation, halogenation, polymerization, reaction-absorption, and reaction-extraction are primarily heterogeneous reaction-separation processes, they present challenges related to "three transmissions and one reaction" and transfer intensification. Relevant chemical process intensification methods and technologies include high-gravity technology, micro-interface technology, ultrasound technology, microwave technology, micro-chemical technology, and rotating disk reaction technology, promoting high-quality, green development of chemical production processes with energy conservation and emission reduction.

[0003] 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 alkylate oil products and is highly demanding. The sulfuric acid-catalyzed C4 alkylation reaction is a rapid, complex, liquid-liquid two-phase process. Improving the mixing state and mass transfer between the acid and hydrocarbon phases is crucial for improving alkylate oil product quality. High-gravity technology excels in enhancing micro-mixing and mass transfer, and has become a key technology for C4 alkylation process intensification. The following patents have been applied for for C4 alkylation:

[0004] 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 comprises: a C4 feedstock is introduced into an alkylation reactor; isobutane and butene are subjected to an alkylation reaction under the action of a sulfuric acid catalyst; the reaction stream is subjected to gas-liquid separation to obtain light hydrocarbons and a liquid stream; the light hydrocarbons are removed from the gas compressor system as a refrigerant; the liquid stream is introduced into a primary acid-hydrocarbon separator; the separated sulfuric acid is returned to the alkylation reactor for recycling; the separated crude reaction product is subjected to a secondary acid-hydrocarbon separation to remove trace acid, and then enters a product fractionation unit for further separation to obtain isobutane, n-butane, and an alkylate oil product; the separated isobutane is returned to the alkylation reactor for further reaction.

[0005] CN209128343 U discloses an experimental apparatus for C4 alkylation. The experimental apparatus comprises: a feeding device, a reaction device, and a separation and recovery device. The feeding device comprises a C4 alkane steel cylinder, a C4 olefin steel cylinder, a C4 alkane feed tank, a C4 olefin feed tank, and a raw material premixing tank. The C4 alkane steel cylinder is connected to the C4 alkane feed tank, the C4 olefin steel cylinder is connected to the C4 olefin feed tank, the C4 alkane feed tank is connected to the raw material premixing tank, and the C4 olefin feed tank is connected to the raw material premixing tank. The reaction device is connected to the raw material premixing tank. The separation and recovery device comprises an alkylation gasoline separation tank, an exhaust gas condensation tank, and a waste acid collection tank. The reaction device is connected to the alkylation gasoline separation tank, the alkylation gasoline separation tank is connected to the exhaust gas condensation tank, and the alkylation gasoline separation tank is connected to the waste acid collection tank.

[0006] CN106542951 A discloses a method for reducing the amount of sulfuric acid used in an alkylation reaction by using a high-efficiency adsorbent. This method can reduce the amount of sulfuric acid used in the production of isooctane from C4. The method is as follows: an alkylation moisture adsorbent is dried and added to an alkylation reactor, followed by addition of 98 wt% sulfuric acid. Dehydrated C4 is then added and subjected to an alkylation reaction at 3°C. When the measured sulfuric acid content is less than 90%, the reaction is stopped, and the waste acid and adsorbent are separated in a separation tank; the adsorbent is transported to an adsorbent regeneration workshop and reused after passing regeneration.

[0007] CN112662426 A discloses a liquid acid alkylation reaction method and apparatus. The apparatus comprises a reactor, a separator, a primary coalescer, a secondary coalescer, a deisobutanizer, a compressor, a waste acid pump, an acid circulation pump, a pipeline mixer, and a raw material pipeline. The raw material pipeline is connected to the reactor via a raw material inlet, and the reactor discharge is connected to the deisobutanizer via the feed inlets of the separator, the primary coalescer, and the secondary coalescer. The method comprises: an alkylation reaction of the raw materials in a reactor using sulfuric acid and fuming sulfuric acid as catalysts, and the reaction products are separated to obtain alkylated gasoline. The alkylation reaction temperature is 15-40°C, the reaction pressure is 0.1-1 MPa, and the contact time in the reactor is 0.2-15 minutes.

[0008] CN112473723 A discloses a high-acid catalyst, a preparation method, and a method for a C4 alkylation reaction. The catalyst comprises a molecular sieve and an aluminum sol, wherein the weight ratio of the molecular sieve to the aluminum sol is 99:1 to 20:80 on a dry basis; and the average particle size of the aluminum sol is less than 20 nm.

[0009] CN107974280 A discloses a liquid acid alkylation reaction method. The alkylation reactor used comprises, from top to bottom, a light phase separation zone (I), a reaction zone (III), a circulation zone (II) and a heavy phase settling zone (IV), wherein the reaction zone (III) and the circulation zone (II) are connected at both ends, a dispersed phase feeder (4) is provided at the bottom of the reaction zone (III), and a continuous phase inlet (1) is provided in the circulation zone (II) on the side wall of the reactor; the reaction zone and the circulation zone are a reaction mixture of a liquid acid catalyst, a mixture of isoparaffins and olefins enters the reaction zone through the dispersed phase feeder, an alkylation reaction occurs between the isoparaffins and olefins under alkylation reaction conditions, and after the reaction, enters the circulation zone, wherein the light phase enters the light phase separation zone at the upper part of the reactor, and the heavy phase enters the heavy phase settling zone at the lower part of the reactor, the alkylation reaction product is extracted from the light phase outlet, and the waste liquid catalyst is extracted from the heavy phase outlet.

[0010] The above patents all utilize specialized mechanical equipment and precision instruments to generate super / microgravity-microinterface, ultrasonic waves, microwaves, and turntable effects to enhance the chemical transfer process, resulting in relatively high energy consumption, equipment investment, and operational difficulty. Summary of the Invention

[0011] The purpose of the present invention is to provide a self-rotating bed super / microgravity-microinterface reaction device and a method for using the same, thereby overcoming the shortcomings of the prior art in that special mechanical equipment and precision instruments are required to generate super / microgravity-microinterface effects to enhance the chemical transfer process, resulting in high energy consumption, equipment investment and operational difficulty.

[0012] To achieve the above-mentioned objectives, the present invention provides a self-rotating bed super / microgravity-microinterface reaction device, comprising: a cylindrical heat exchanger, wherein a first material inlet and a material outlet are respectively provided at its left and right ends, a heat exchange fluid inlet and a heat exchange fluid outlet are respectively provided on the left and right sides of the cylindrical heat exchanger, and at least two second material inlets are provided on the side wall of the cylindrical heat exchanger; a coil reactor, which comprises a coil, wherein the coil is cylindrical and spiral-shaped, the coil is located in the cylindrical heat exchanger, and the axis of the coil is distributed along the left and right directions; the left end of the coil is connected to the first material inlet, and the right end of the coil is connected to the material outlet; two material ports are provided on the coil, each of which is connected to one of the second material inlets; and a fluid conveyor, wherein the first material inlet and the two second material inlets are each connected to one of the fluid conveyors.

[0013] Preferably, in the above technical solution, the number of the second material inlets is at least six, of which four are arranged above the cylindrical heat exchanger and are spaced apart in the left-right direction, and the remaining two are arranged below the cylindrical heat exchanger and are spaced apart in the left-right direction; the coil is provided with the material port at a position corresponding to each second material inlet, and each material port is connected to the corresponding second material inlet.

[0014] Preferably, in the above technical solution, the diameter of the coil is 3 mm to 100 mm, the number of turns of the coil is 1 to 500, and the diameter of each turn of the coil is 50 mm to 1200 mm.

[0015] Preferably, in the above technical solution, the diameter of the cylindrical heat exchanger is 70 mm to 1250 mm, and the length is 500 mm to 60000 mm.

[0016] Preferably, in the above technical solution, two upper and lower rows of baffle groups are provided in the cylindrical heat exchanger, each row of the baffle groups includes a plurality of baffles spaced apart in the left-right direction, and the baffles of the two rows of the baffle groups are staggered with each other.

[0017] Preferably, in the above technical solution, the distance between two adjacent baffles is 50 mm to 500 mm.

[0018] A method for using the above-mentioned rotating bed super / microgravity-microinterface reaction device comprises the following steps:

[0019] 1) The reaction device is used for alkylation reaction, and 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 connected to the first material inlet is the first fluid conveyor, and the fluid conveyor connected to the second material inlet is the second fluid conveyor; the first fluid conveyor is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey sulfuric acid or ionic liquid into the coil through the first material inlet; the two second fluid conveyors are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes into the coil through the corresponding second material inlets; and the reaction materials conveyed by the fluid conveyors have a reaction material flow rate determined by the size of the β value, so that the sulfuric acid or ionic liquid flow rate V of the first material inlet, the C4 olefin flow rate V of the second material inlet, and the C4 alkanes flow rate V of the other second material inlet all satisfy formula (3); the specific calculation formula is as follows:

[0020] Centrifugal acceleration is G = Rω 2 (1)

[0021] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0022] Hypergravity / microgravity factors

[0023] Where: G-centrifugal acceleration, m / s 2 ;

[0024] R-circular motion radius, that is, the radius of each circle of the coil, m;

[0025] g-Earth's gravitational acceleration, m / s 2 ;

[0026] ω-angular velocity of circular motion, that is, the angular velocity of the material moving in the coil, 1 / s;

[0027] β-hyper / microgravity factor;

[0028] N-circular motion speed, r / min;

[0029] π - pi;

[0030] V-circular motion linear velocity, that is, the flow rate of the material in the coil, m / s;

[0031] Where R is a known value, and β takes a specific value so that the material is in a slightly heavy or overweight state in the coil reactor;

[0032] 2) The sulfuric acid or ionic liquid flowing in from the first material inlet, the C4 olefin flowing in from the second material inlet, and the C4 alkane flowing in from another second material inlet are mixed and alkylated in the coil.

[0033] Among them, when β=1~50, it is the microgravity field effect; when β>50, it is the hypergravity field effect. The β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material.

[0034] Compared with the prior art, the present invention has the following beneficial effects:

[0035] 1. The reaction materials of the present invention are pressurized by a fluid conveyor and fed into a coil-type reactor. The materials rotate circumferentially in the reactor, generating centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, gravity can be overcome to form a super / microgravity-microinterface field, thereby forming millimeter-scale or micron-scale droplets and bubbles in the heterogeneous reaction materials. The collective scale of the gas-liquid, gas-liquid-liquid, and gas-liquid-solid interfaces is efficiently regulated from the milli-centimeter level to the micron level, thereby enhancing the mixing between the fluid phases and the synergistic coupling effect of the reaction process, thereby achieving an enhanced transfer effect of the reaction system. There is no need to use special mechanical equipment to drive the reaction materials to rotate at high speed to generate centrifugal force. Instead, the reaction materials rotate circumferentially in the reaction device to generate super / microgravity-microinterface to achieve the enhanced transfer process of the reaction system. The structure is simple, easy to manufacture, reliable in operation, convenient to install and maintain, and easy to operate, and can achieve the goals of high efficiency, low energy consumption, low pollution, and low investment in industrial production.

[0036] 2. The reaction apparatus of the present invention is simple and convenient to use. It can enable a variety of materials to flow in a circular rotation within the coil while maintaining a super / microgravity-microinterface field state for mixing and performing an alkylation reaction, thereby increasing the gas-liquid phase transfer area of the reaction system and promoting the reaction progress. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Figure 1 It is a structural schematic diagram of the self-rotating bed super / microgravity-microinterface reaction device according to the present invention.

[0038] Figure 2 Schematic diagram of the structure of the coil reactor according to the present invention.

[0039] Figure 3 According to the present invention Figure 2 Schematic diagram of the left side.

[0040] Figure 4 It is a structural schematic diagram of a self-rotating bed super / microgravity-microinterface reaction device for alkylation reaction according to the present invention.

[0041] Description of main reference numerals:

[0042] 1-first material inlet, 2-coil, 3-heat exchange fluid inlet, 4-material outlet, 5-baffle, 6-cylindrical heat exchanger, 7-second material inlet, 8-second fluid conveyor, 9-heat exchange fluid outlet, 10-first fluid conveyor, 11-material outlet. DETAILED DESCRIPTION

[0043] The specific embodiments of the present invention are described in detail below with reference to the accompanying drawings, but it should be understood that the protection scope of the present invention is not limited by the specific embodiments.

[0044] 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.

[0045] Example 1

[0046] Figures 1 to 4 The schematic diagram of the structure of a self-rotating bed super / microgravity-micro interface reaction device according to a preferred embodiment of the present invention is shown. The reaction device includes a cylindrical heat exchanger 6, a coil reactor and a fluid conveyor. Figures 1 to 4 The cylindrical heat exchanger 6 has a first material inlet 1 and a material outlet 4 on its left and right ends, respectively. It also has a heat exchange fluid inlet 3 and a heat exchange fluid outlet 9 on its left and right sides, respectively. The reaction takes place within the cylindrical heat exchanger 6, releasing or absorbing heat during the reaction. Cold or hot fluids flow in and out of the cylindrical heat exchanger 6 to control the reaction temperature. The heat exchange fluid inlet 3 is preferably located below the cylindrical heat exchanger 6, while the heat exchange fluid outlet 9 is preferably located above it. At least two second material inlets 7 are provided on the sidewalls of the cylindrical heat exchanger 6 to facilitate the addition of reactants. The coil-and-tube reactor includes a coil 2, which is cylindrical and spiral in shape, increasing the heat exchange area and allowing the material within the coil 2 to flow in a circular motion. The coil 2 is located within the cylindrical heat exchanger 6, with its axis running in the left-right direction. The left end of the coil 2 is connected to the first material inlet 1, and the right end is connected to the material outlet 4. The coil 2 is provided with two material ports 11, each of which is connected to a second material inlet 7, so that multiple materials can be mixed in the coil 2. The first material inlet 1 and the two second material inlets 7 are each connected to a fluid conveyor, which is used to convey materials and can also adjust the flow rate of each material. The reaction material is pressurized by the fluid conveyor and sent into the coil reactor at high speed. The reaction material is pressurized by the fluid conveyor and sent into the coil reactor at high speed. The material performs a circular rotation flow in the reactor to generate centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, it can overcome gravity to form a super / microgravity-micro interface field, so that the heterogeneous reaction materials form millimeter-level or micrometer-level small droplets and small bubbles, and the collective scale of the gas-liquid, gas-liquid-liquid, and gas-liquid-solid interfaces is efficiently regulated from the milli-centimeter level to the micrometer level to enhance the fluid phase. The inter-mixing and reaction process synergistically couple to achieve the transmission effect of the enhanced reaction system. It does not require any power components and equipment and has the advantages of simple structure, easy manufacturing, reliable operation, convenient installation and maintenance, and simple operation, thereby achieving the industrial production goals of high efficiency, low energy consumption, low pollution and low investment. The reaction device can be widely used in heterogeneous reaction-separation processes such as redox, catalytic hydrogenation, esterification, condensation, alkylation, sulfonation, halogenation, polymerization, reaction-absorption, reaction-extraction, reaction-crystallization and liquid-liquid extraction, and has strong practicality.

[0047] refer to Figure 4 Preferably, the number of second material inlets 7 is at least six, of which four are located above the cylindrical heat exchanger 6 and spaced apart in the left-right direction, and the remaining two are located below the cylindrical heat exchanger 6 and spaced apart in the left-right direction. The coil 2 is provided with a material port 11 at a position corresponding to each second material inlet 7, and each material port 11 is connected to the corresponding second material inlet 7. When the reaction apparatus is used for an alkylation reaction, the number of fluid conveyors is three: the fluid conveyor connected to the first material inlet 1 is used to convey sulfuric acid or an ionic liquid; the other two fluid conveyors are used to convey C4 olefins and C4 alkanes, respectively. Among them, the first second material inlet 7 located at the top and counted from left to right, the third second material inlet 7, and the second second material inlet 7 located at the bottom and counted from left to right are all connected to a fluid conveyor for conveying four carbon olefins; the second second material inlet 7 located at the top and counted from left to right, the fourth second material inlet 7, and the first second material inlet 7 located at the bottom and counted from left to right are all connected to a fluid conveyor for conveying four carbon alkanes, so that four carbon olefins and four carbon alkanes can be added to the coil 2 at different positions of the coil 2, so that the reaction materials can be fully mixed and reacted.

[0048] refer to Figures 1 to 4 Preferably, the diameter of the coil 2 is 3 mm to 100 mm, the number of turns of the coil 2 is 1 to 500 turns, and the diameter of each turn of the coil 2 is 50 mm to 1200 mm.

[0049] refer to Figures 1 to 4 Preferably, the diameter of the cylindrical heat exchanger 6 is 70 mm to 1250 mm, and the length is 500 mm to 60000 mm.

[0050] refer to Figure 1 and Figure 4 Preferably, the cylindrical heat exchanger 6 is provided with two upper and lower rows of baffle plates. Each row includes a plurality of baffle plates 5 spaced apart in the left-right direction. The baffle plates 5 in the two rows are staggered to guide the flow of the cooling or heating fluid within the cylindrical heat exchanger 6 and improve the heat exchange effect. Furthermore, preferably, the distance between two adjacent baffle plates 5 is 50 mm to 500 mm.

[0051] Example 2

[0052] refer to Figures 1 to 4 , using the self-rotating bed super / microgravity-microinterface reaction device of Example 1 as a reaction device, a method for using the self-rotating bed super / microgravity-microinterface reaction device, the operating steps are as follows:

[0053] 1) This reaction apparatus is used for an alkylation reaction. The heat exchange fluid inlet 3 and outlet 9 of a cylindrical heat exchanger 6 are connected to a device for supplying a cooling fluid. The cylindrical heat exchanger 6 has a diameter of 140 mm and a length of 800 mm. Seven baffles 5 are installed within the cylindrical heat exchanger 6, with a distance of 100 mm between adjacent baffles 5. These baffles are used to cool the reactants within the coil 2. The coil 2 has a diameter of 6 mm and 10 turns, each with a diameter of 100 mm. The fluid conveyor connected to the first material inlet 1 is a first fluid conveyor 10, and the fluid conveyor connected to the second material inlet 7 is a second fluid conveyor 8. The first fluid conveyor 10 is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey the sulfuric acid or ionic liquid into the coil 2 through the first material inlet 1; the two second fluid conveyors 8 are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes into the coil 2 through the corresponding second material inlets 7. The reaction material conveyed by the fluid conveyor has a flow rate V determined by the value of β. Through the action of the fluid conveyor, the flow rate of each reaction material is controlled to 2.22 m / s, so that the flow rate V of sulfuric acid or ionic liquid at the first material inlet 1, the flow rate V of C4 olefins at the second material inlet 7, and the flow rate V of C4 alkanes at the other second material inlet 7 all meet formula (3); the specific calculation formula is as follows:

[0054] Centrifugal acceleration is G = Rω 2 (1)

[0055] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0056] Hypergravity / microgravity factors

[0057] Where: G-centrifugal acceleration, m / s 2 ; R-circular motion radius, that is, the radius of each coil, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, that is, the angular velocity of the material moving in the coil, 1 / s;β-super / microgravity factor;N-circular motion speed, r / min;π-pi;V-circular motion linear velocity, that is, the flow rate of the material in the coil, m / s.

[0058] Among them, β and r are known values, and β takes a specific value so that the material is in a microgravity or supergravity state in the fluid reactor; when the centrifugal acceleration G is 1 to 50 times the earth's gravitational acceleration g, that is, β = 1 to 50, it is a microgravity field effect; when the centrifugal acceleration G is greater than 50 times the earth's gravitational acceleration g, that is, β>50, it is a supergravity field effect, and the β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material; under the super / microgravity field, the material causes the heterogeneous reaction materials to form millimeter-level or micron-level droplets and small bubbles, effectively promoting the mixing between the heterogeneous reaction materials and enhancing the transfer process.

[0059] Specifically, each reaction material is in a slightly heavy state after entering the coil 2, and β=10. At this time, G=98.1m / s 2 , V = 2.22 m / s, which is the speed at which the above-mentioned reaction materials (sulfuric acid or ionic liquid, C4 olefin, C4 olefin) enter the coil 2.

[0060] 2) The sulfuric acid or ionic liquid flowing in from the first material inlet 1, the C4 olefin flowing in from the second material inlet 7, and the C4 alkane flowing in from another second material inlet 7 rotate in a circular motion within the coil 2, generating centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, gravity can be overcome to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, the sulfuric acid or ionic liquid, the C4 olefin, and the C4 alkane are fully mixed and reacted. After the reaction is completed, the resulting reactants are discharged from the material outlet 4. During the reaction, a cold fluid enters from the heat exchange fluid inlet 3, completes heat exchange with the reaction materials in the coil 2, and then flows out through the heat exchange fluid outlet 9 to cool the reaction materials in the coil 2.

[0061] Example 3

[0062] refer to Figure 1 and Figure 4 , using the self-rotating bed super / microgravity-microinterface reaction device of Example 1 as a reaction device, a method for using the self-rotating bed super / microgravity-microinterface reaction device, the operating steps are as follows:

[0063] 1), this reaction apparatus is used for an alkylation reaction. The heat exchange fluid inlet 3 and heat exchange fluid outlet 9 of a cylindrical heat exchanger 6 are connected to a device for providing a cold fluid. The cylindrical heat exchanger 6 has a diameter of 240 mm and a length of 1600 mm. Seven baffles 5 are installed within the cylindrical heat exchanger 6, with a distance of 200 mm between adjacent baffles 5, to cool the reactants within the coil 2. The coil 2 has a diameter of 10 mm and 20 turns, each with a diameter of 200 mm. The fluid conveyor connected to the first material inlet 1 is a first fluid conveyor 10, and the fluid conveyor connected to the second material inlet 7 is a second fluid conveyor 8. The first fluid conveyor 10 is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey sulfuric acid or ionic liquid into the coil 2 through the first material inlet 1; the two second fluid conveyors 8 are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes into the coil 2 through the corresponding second material inlets 7. The reaction material conveyed by the fluid conveyor has a flow rate V determined by the value of β. Through the action of the fluid conveyor, the flow rate of each reaction material is controlled to 5.88 m / s. So that the flow rate V of sulfuric acid or ionic liquid at the first material inlet 1, the flow rate V of C4 olefins at the second material inlet 7, and the flow rate V of C4 alkanes at the other second material inlet 7 all meet formula (3); the specific calculation formula is as follows:

[0064] Centrifugal acceleration is G = Rω 2 (1)

[0065] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0066] Hypergravity / microgravity factors

[0067] Where: G-centrifugal acceleration, m / s 2 ; R-circular motion radius, that is, the radius of each coil, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, that is, the angular velocity of the material moving in the coil, 1 / s;β-super / microgravity factor;N-circular motion speed, r / min;π-pi;V-circular motion linear velocity, that is, the flow rate of the material in the coil, m / s.

[0068] Among them, β and r are known values, and β takes a specific value so that the material is in a microgravity or supergravity state in the fluid reactor; when the centrifugal acceleration G is 1 to 50 times the earth's gravitational acceleration g, that is, β = 1 to 50, it is a microgravity field effect; when the centrifugal acceleration G is greater than 50 times the earth's gravitational acceleration g, that is, β>50, it is a supergravity field effect, and the β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material; under the super / microgravity field, the material causes the heterogeneous reaction materials to form millimeter-level or micron-level droplets and small bubbles, effectively promoting the mixing between the heterogeneous reaction materials and enhancing the transfer process.

[0069] Specifically, each reaction material is in a slightly heavy state after entering the coil 2, and β is set to 35. At this time, G = 343.35 m / s 2 , V = 5.88 m / s, which is the speed at which the above-mentioned reaction materials (sulfuric acid or ionic liquid, C4 olefin, C4 olefin) enter the coil 2.

[0070] 2) The sulfuric acid or ionic liquid flowing in from the first material inlet 1, the C4 olefin flowing in from the second material inlet 7, and the C4 alkane flowing in from another second material inlet 7 rotate in a circular motion within the coil 2, generating centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, gravity can be overcome to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, the sulfuric acid or ionic liquid, the C4 olefin, and the C4 alkane are fully mixed and reacted. After the reaction is completed, the resulting reactants are discharged from the material outlet 4. During the reaction, a cold fluid enters from the heat exchange fluid inlet 3, completes heat exchange with the reaction materials in the coil 2, and then flows out through the heat exchange fluid outlet 9 to cool the reaction materials in the coil 2.

[0071] Example 4

[0072] refer to Figures 1 to 4 , using the self-rotating bed super / microgravity-microinterface reaction device of Example 1 as a reaction device, a method for using the self-rotating bed super / microgravity-microinterface reaction device, the operating steps are as follows:

[0073] 1), this reaction apparatus is used for an alkylation reaction. The heat exchange fluid inlet 3 and heat exchange fluid outlet 9 of a cylindrical heat exchanger 6 are connected to a device for providing a cold fluid. The cylindrical heat exchanger 6 has a diameter of 550 mm and a length of 6000 mm. It is equipped with 14 baffles 5, with a distance of 400 mm between adjacent baffles 5, for cooling the reactants within the coil 2. The coil 2 has a diameter of 40 mm and 100 turns, each with a diameter of 500 mm. The fluid conveyor connected to the first material inlet 1 is a first fluid conveyor 10, and the fluid conveyor connected to the second material inlet 7 is a second fluid conveyor 8. The first fluid conveyor 10 is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey the sulfuric acid or ionic liquid into the coil 2 through the first material inlet 1; the two second fluid conveyors 8 are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes into the coil 2 through the corresponding second material inlets 7. The reaction material conveyed by the fluid conveyor has a flow rate V determined by the value of β. Through the action of the fluid conveyor, the flow rate of each reaction material is controlled to 12.66 m / s, so that the flow rate V of sulfuric acid or ionic liquid at the first material inlet 1, the flow rate V of C4 olefins at the second material inlet 7, and the flow rate V of C4 alkanes at the other second material inlet 7 all meet formula (3); the specific calculation formula is as follows:

[0074] Centrifugal acceleration is G = Rω 2 (1)

[0075] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0076] Hypergravity / microgravity factors

[0077] Where: G-centrifugal acceleration, m / s 2 ; R-circular motion radius, that is, the radius of each coil, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, that is, the angular velocity of the material moving in the coil, 1 / s;β-super / microgravity factor;N-circular motion speed, r / min;π-pi;V-circular motion linear velocity, that is, the flow rate of the material in the coil, m / s.

[0078] Among them, β and r are known values, and β takes a specific value so that the material is in a microgravity or supergravity state in the fluid reactor; when the centrifugal acceleration G is 1 to 50 times the earth's gravitational acceleration g, that is, β = 1 to 50, it is a microgravity field effect; when the centrifugal acceleration G is greater than 50 times the earth's gravitational acceleration g, that is, β>50, it is a supergravity field effect, and the β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material; under the super / microgravity field, the material causes the heterogeneous reaction materials to form millimeter-level or micron-level droplets and small bubbles, effectively promoting the mixing between the heterogeneous reaction materials and enhancing the transfer process.

[0079] Specifically, each reaction material is in an overweight state after entering the coil 2, and β is set to 65. At this time, G = 637.65 m / s 2 , V = 12.66 m / s, which is the speed at which the above-mentioned reaction materials (sulfuric acid or ionic liquid, C4 olefin, C4 olefin) enter the coil 2.

[0080] 2) The sulfuric acid or ionic liquid flowing in from the first material inlet 1, the C4 olefin flowing in from the second material inlet 7, and the C4 alkane flowing in from another second material inlet 7 rotate in a circular motion within the coil 2, generating centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, gravity can be overcome to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, the sulfuric acid or ionic liquid, the C4 olefin, and the C4 alkane are fully mixed and reacted. After the reaction is completed, the resulting reactants are discharged from the material outlet 4. During the reaction, a cold fluid enters from the heat exchange fluid inlet 3, completes heat exchange with the reaction materials in the coil 2, and then flows out through the heat exchange fluid outlet 9 to cool the reaction materials in the coil 2.

[0081] Example 5

[0082] refer to Figure 1 and Figure 4 , using the self-rotating bed super / microgravity-microinterface reaction device of Example 1 as a reaction device, a method for using the self-rotating bed super / microgravity-microinterface reaction device, the operating steps are as follows:

[0083] 1), this reaction apparatus is used for an alkylation reaction. The heat exchange fluid inlet 3 and heat exchange fluid outlet 9 of a cylindrical heat exchanger 6 are connected to a device for providing a cold fluid. The cylindrical heat exchanger 6 has a diameter of 960 mm and a length of 35,000 mm. It is equipped with 69 baffles 5, with a distance of 500 mm between adjacent baffles 5, for cooling the reactants within the coil 2. The coil 2 has a diameter of 10 mm and 400 coils, each with a diameter of 900 mm. The fluid conveyor connected to the first material inlet 1 is a first fluid conveyor 10, and the fluid conveyor connected to the second material inlet 7 is a second fluid conveyor 8. The first fluid conveyor 10 is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey the sulfuric acid or ionic liquid into the coil 2 through the first material inlet 1; the two second fluid conveyors 8 are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes into the coil 2 through the corresponding second material inlets 7. The reaction material conveyed by the fluid conveyor has a flow rate V determined by the value of β. Through the action of the fluid conveyor, the flow rate of each reaction material is controlled to 21.59 m / s, so that the flow rate V of sulfuric acid or ionic liquid at the first material inlet 1, the flow rate V of C4 olefins at the second material inlet 7, and the flow rate V of C4 alkanes at the other second material inlet 7 all meet formula (3); 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, that is, the radius of each coil, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, that is, the angular velocity of the material moving in the coil, 1 / s;β-super / microgravity factor;N-circular motion speed, r / min;π-pi;V-circular motion linear velocity, that is, the flow rate of the material in the coil, m / s.

[0088] Among them, β and r are known values, and β takes a specific value so that the material is in a microgravity or supergravity state in the fluid reactor; when the centrifugal acceleration G is 1 to 50 times the earth's gravitational acceleration g, that is, β = 1 to 50, it is a microgravity field effect; when the centrifugal acceleration G is greater than 50 times the earth's gravitational acceleration g, that is, β>50, it is a supergravity field effect, and the β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material; under the super / microgravity field, the material causes the heterogeneous reaction materials to form millimeter-level or micron-level droplets and small bubbles, effectively promoting the mixing between the heterogeneous reaction materials and enhancing the transfer process.

[0089] Specifically, each reaction material is in an overweight state after entering the coil 2, and β=105. At this time, G=1030.05m / s 2 , V = 21.59 m / s, which is the speed at which the above-mentioned reaction materials (sulfuric acid or ionic liquid, C4 olefin, C4 olefin) enter the coil 2.

[0090] 2) The sulfuric acid or ionic liquid flowing in from the first material inlet 1, the C4 olefin flowing in from the second material inlet 7, and the C4 alkane flowing in from another second material inlet 7 rotate in a circular motion within the coil 2, generating centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, gravity can be overcome to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, the sulfuric acid or ionic liquid, the C4 olefin, and the C4 alkane are fully mixed and reacted. After the reaction is completed, the resulting reactants are discharged from the material outlet 4. During the reaction, a cold fluid enters from the heat exchange fluid inlet 3, completes heat exchange with the reaction materials in the coil 2, and then flows out through the heat exchange fluid outlet 9 to cool the reaction materials in the coil 2.

[0091] Example 6

[0092] refer to Figure 1 and Figure 4 , using the self-rotating bed super / microgravity-microinterface reaction device of Example 1 as a reaction device, a method for using the self-rotating bed super / microgravity-microinterface reaction device, the operating steps are as follows:

[0093] 1), this reaction apparatus is used for an alkylation reaction. The heat exchange fluid inlet 3 and heat exchange fluid outlet 9 of a cylindrical heat exchanger 6 are connected to a device for providing a cold fluid. The cylindrical heat exchanger 6 has a diameter of 1250 mm and a length of 5000 mm. Nine baffles 5 are installed within the cylindrical heat exchanger 6, with a distance of 500 mm between adjacent baffles 5, to cool the reactants within the coil 2. The coil 2 has a diameter of 100 mm and 30 coils, each with a diameter of 1200 mm. The fluid conveyor connected to the first material inlet 1 is a first fluid conveyor 10, and the fluid conveyor connected to the second material inlet 7 is a second fluid conveyor 8. The first fluid conveyor 10 is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey the sulfuric acid or ionic liquid into the coil 2 through the first material inlet 1; the two second fluid conveyors 8 are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes into the coil 2 through the corresponding second material inlets 7. The reaction material conveyed by the fluid conveyor has a flow rate V determined by the value of β. Through the action of the fluid conveyor, the flow rate of each reaction material is controlled to 32.65 m / s, so that the flow rate V of sulfuric acid or ionic liquid at the first material inlet 1, the flow rate V of C4 olefins at the second material inlet 7, and the flow rate V of C4 alkanes at the other second material inlet 7 all meet formula (3); the specific calculation formula is as follows:

[0094] Centrifugal acceleration is G = Rω 2 (1)

[0095] The acceleration due to gravity of the earth is g = 9.81 m / s 2 (2)

[0096] Hypergravity / microgravity factors

[0097] Where: G-centrifugal acceleration, m / s 2 ; R-circular motion radius, that is, the radius of each coil, m; g-earth gravity acceleration, m / s 2 ;ω-angular velocity of circular motion, that is, the angular velocity of the material moving in the coil, 1 / s;β-super / microgravity factor;N-circular motion speed, r / min;π-pi;V-circular motion linear velocity, that is, the flow rate of the material in the coil, m / s.

[0098] Among them, β and r are known values, and β takes a specific value so that the material is in a microgravity or supergravity state in the fluid reactor; when the centrifugal acceleration G is 1 to 50 times the earth's gravitational acceleration g, that is, β = 1 to 50, it is a microgravity field effect; when the centrifugal acceleration G is greater than 50 times the earth's gravitational acceleration g, that is, β>50, it is a supergravity field effect, and the β value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the material; under the super / microgravity field, the material causes the heterogeneous reaction materials to form millimeter-level or micron-level droplets and small bubbles, effectively promoting the mixing between the heterogeneous reaction materials and enhancing the transfer process.

[0099] Specifically, each reaction material is in an overweight state after entering the coil, and β=180. At this time, G=1765.8m / s 2 , V = 32.65 m / s, which is the speed at which the above-mentioned reaction materials (sulfuric acid or ionic liquid, C4 olefin, C4 olefin) enter the coil 2.

[0100] 2) The sulfuric acid or ionic liquid flowing in from the first material inlet 1, the C4 olefin flowing in from the second material inlet 7, and the C4 alkane flowing in from another second material inlet 7 rotate in a circular motion within the coil 2, generating centrifugal force. Under the action of the centrifugal force generated by the high-speed self-rotating flow, gravity can be overcome to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, the sulfuric acid or ionic liquid, the C4 olefin, and the C4 alkane are fully mixed and reacted. After the reaction is completed, the resulting reactants are discharged from the material outlet 4. During the reaction, a cold fluid enters from the heat exchange fluid inlet 3, completes heat exchange with the reaction materials in the coil 2, and then flows out through the heat exchange fluid outlet 9 to cool the reaction materials in the coil 2.

[0101] 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 self-rotating bed super / microgravity-microinterface reaction device, characterized in that: include: A cylindrical heat exchanger having a first material inlet and a material outlet at its left and right ends, respectively; a heat exchange fluid inlet and a heat exchange fluid outlet at its left and right sides, respectively; and at least two second material inlets on the sidewalls of the cylindrical heat exchanger; two upper and lower rows of baffle groups are provided within the cylindrical heat exchanger, each row of the baffle groups including a plurality of baffles spaced apart in the left-right direction, and the baffles of the two rows of the baffle groups are staggered; A coil-type reactor, comprising a coil, the coil being cylindrical and spiral, located within the cylindrical heat exchanger, with the axis of the coil extending in the left-right direction; the left end of the coil being connected to the first material inlet, and the right end of the coil being connected to the material outlet; the coil being provided with two material ports, each connected to one of the second material inlets; the coil having a diameter of 3 mm to 100 mm, the number of coil turns being 1 to 500, and the diameter of each coil being 50 mm to 1200 mm; and The fluid conveyor, the first material inlet and the two second material inlets are each connected to one of the fluid conveyors; the fluid conveyor connected to the first material inlet is the first fluid conveyor, and the fluid conveyor connected to the second material inlet is the second fluid conveyor; the first fluid conveyor is connected to the device for providing sulfuric acid or ionic liquid, and is used to convey sulfuric acid or ionic liquid to the coil through the first material inlet; the two second fluid conveyors are respectively connected to the device for providing C4 olefins and the device for providing C4 alkanes, and are used to convey C4 olefins and C4 alkanes to the coil through the corresponding second material inlets; and the reaction materials conveyed by the fluid conveyor are β The value determines the flow rate of the reaction materials so that the flow rate of sulfuric acid or ionic liquid at the first material inlet is V , C4 olefin flow rate at the second material inlet V and the flow rate of the carbon tetraalkane at the second material inlet V All satisfy formula (3); the specific calculation formula is as follows: The centrifugal acceleration is (1) The acceleration due to gravity of the Earth is (2) Hypergravity / microgravity factors (3) Where: G -Centrifugal acceleration, m / s 2 ;R-circular motion radius, m; g -Earth's gravitational acceleration, m / s 2 ; ω - angular velocity of circular motion, 1 / s; β - Hyper / microgravity factor; N -Circular motion speed, r / min; π - pi; V -Linear velocity of circular motion, m / s.

2. The rotating bed super / microgravity-microinterface reaction device according to claim 1, characterized in that: The number of the second material inlets is at least six, four of which are arranged above the cylindrical heat exchanger and spaced apart in the left-right direction, and the remaining two are arranged below the cylindrical heat exchanger and spaced apart in the left-right direction; the coil is provided with a material port at a position corresponding to each second material inlet, and each material port is connected to the corresponding second material inlet.

3. The self-rotating bed super / microgravity-microinterface reaction device according to claim 1, characterized in that: The diameter of the cylindrical heat exchanger is 70 mm to 1250 mm, and the length is 500 mm to 60000 mm.

4. The rotating bed super / microgravity-microinterface reaction device according to claim 1, characterized in that: The distance between two adjacent baffles is 50 mm to 500 mm.

5. A method for using the rotating bed super / microgravity-microinterface reaction device according to claim 1, characterized in that: The following steps are involved: 1) The reaction device is used for alkylation reaction, and the heat exchange fluid inlet and the heat exchange fluid outlet are connected to a device for providing a cold fluid for heat exchange; 2) The sulfuric acid or ionic liquid flowing in from the first material inlet, the C4 olefin flowing in from the second material inlet, and the C4 alkane flowing in from another second material inlet are mixed and alkylated in the coil.

6. The method for using the rotating bed super / microgravity-microinterface reaction device according to claim 5, characterized in that: when β =1~50 is the microgravity field effect; when β When it is greater than 50, it is the supergravity field effect, which is selected by the viscosity, density, temperature and chemical reaction characteristics of the material. β Value size.

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