Reaction device for spin super / micro-gravity-micro-interface synergistic strengthening of rosin catalytic hydrogenation and use method thereof

Abstract

The application discloses a reaction device for spin rotating super / micro gravity-micro interface synergistically reinforced catalytic hydrogenation of turpentine, which comprises a heat exchanger, the connection mode between the heat exchangers is series connection and parallel connection, that is, series connection combined with parallel connection, the material outlet of the first heat exchanger is communicated with the material inlet of the second heat exchanger, and the material outlet of the Nth heat exchanger is communicated with the material inlets of the N+1th and N+2th heat exchangers, a super / micro gravity-micro interface reactor and a fluid conveyor, wherein the material inlet is communicated with the fluid conveyor. The centrifugal force generated by the self-rotating circumferential flow of the reaction material in the reaction device is utilized to overcome the gravity to form a super / micro gravity-micro interface field, so that the heterogeneous reaction material is formed into millimeter or micrometer droplets and small bubbles, the collection scale of the gas-liquid-solid interface is efficiently regulated from the millimeter level to the micrometer level, and the mixing and transfer process of the heterogeneous reaction material are efficiently promoted.

Description

Technical Field

[0001] This invention relates to the field of chemical production equipment technology, specifically to a reaction apparatus and its method of use that synergistically enhances the catalytic hydrogenation of rosin through self-rotation, ultra / microgravity, and micro-interface. Background Technology

[0002] Pine resin, a secretion of pine trees, is known as "oil growing on trees" and is one of the largest biomass oil resources. Pine resin is distilled to obtain rosin and turpentine oil. Rosin is a mixture of thirteen resin acids, small amounts of fatty acids, and some neutral substances. Because rosin resin acids contain conjugated double bonds, rosin is easily oxidized by oxygen in the air. The main components of turpentine oil are α-pinene and β-pinene, along with small amounts of sesquiterpenes, namely longifolene and caryophyllene. Catalytic hydrogenation of pine resin involves the hydrogenation reaction of turpentine oil and rosin. The hydrogenation of turpentine oil mainly involves the reaction of pinene to produce pinane, which is an important intermediate in the synthesis of pharmaceuticals, fragrances, adhesives, and other fine chemical products. The product obtained from the hydrogenation reaction of rosin is hydrogenated rosin, which has advantages such as good antioxidant properties, low brittleness, high thermal stability, and light color. Due to the steric hindrance of the tricyclic phenanthrene skeleton in rosin abietic resins and the high viscosity of rosin melt, gas-liquid mass transfer is difficult. Therefore, the hydrogenation reaction requires high temperature and pressure, and the use of the noble metal Pd / C as a catalyst. In the prior art, CN201310673150.4 discloses an apparatus and method for collecting rosin and preparing hydrocarbon liquid fuels. This apparatus collects resin from within the plant, without damaging the plant, resulting in high labor productivity and high-quality rosin. Hydrocarbon liquid fuels are obtained through a hydrogenation reactor, allowing collection and processing to occur simultaneously, improving rosin utilization and labor productivity. CN201110289747.X provides a simple, time-efficient, and mild synthesis process for hydrogenated rosin. CN200410078371.8 discloses a new method for manufacturing water-white hydrogenated rosin. It first uses sterilized, low-oxygen water to rinse the rosin, removing impurities such as gum, chlorophyll, trace sugars, and proteins. CN01128415.3 discloses a method using rosin dissolved in rosin liquid or 200# solvent oil as raw material, employing skeletal nickel as a catalyst. Its main feature is the use of non-precious metal nickel as a catalyst, which significantly reduces the production cost of hydrogenated rosin. It also has advantages such as mild hydrogenation reaction conditions, short process flow, low investment, easy operation, and flexible production. CN98115885.4 discloses a method using rosin or rosin dissolved in a solvent as raw material. This invention features a short hydrogenation reaction time, long catalyst lifespan, and stable operation. CN93118671.4 A method for producing dihydro or tetrahydrorosin (hereinafter referred to as hydrogenated rosin) from rosin as raw material. The method has a low reaction temperature and pressure, does not require high vacuum distillation, produces high-quality products, has low cost, and is in line with national conditions.

[0003] The aforementioned invention applications all utilize mechanical equipment and precision instruments to generate supergravity, micro-interfaces, ultrasound, microwaves, and turntable effects to enhance chemical transfer processes, resulting in higher energy consumption, equipment investment, and operational difficulties. Summary of the Invention

[0004] To address the aforementioned technical problems, this invention provides a reaction apparatus and its method for enhancing the catalytic hydrogenation of rosin through a self-rotating ultra / microgravity-microinterface synergistic enhancement. The apparatus utilizes the centrifugal force generated by the rotational flow of the reactants to overcome the gravitational field and form an ultra / microgravity field, thereby achieving convenient operation, energy saving, reduced consumption, and lower equipment investment costs.

[0005] To achieve the above objectives, the technical solution provided by the present invention is as follows:

[0006] A self-rotating, microgravity-microinterface synergistic enhancement device for the catalytic hydrogenation of rosin, the device comprising:

[0007] The heat exchanger has a material inlet and a material outlet at its upper and lower ends, respectively. The side wall of the heat exchanger has a heat exchange fluid inlet and a heat exchange fluid outlet. There are four or more heat exchangers. The heat exchangers are connected in a series-parallel connection, that is, a series-parallel connection. The material outlet of the first heat exchanger is connected to the material inlet of the second heat exchanger, and so on, until the material outlet of the Nth heat exchanger is connected to the material inlets of the N+1th and N+2th heat exchangers, and so on.

[0008] A supergravity / microgravity-microinterface reactor is disposed within the heat exchanger. The reactor includes a central fluid tube and fluid distributors. The central fluid tube is a cylindrical tube open at its upper end, and its upper end is connected to the material inlet. At least one fluid distributor is axially arranged on the central fluid tube. Each fluid distributor includes at least three groups of arc-shaped bends, each group comprising at least one arc-shaped bend, and the arc-shaped bends are radially distributed. When the number of arc-shaped bends in each group is ≥2, the arc diameter of the arc-shaped bends increases sequentially from the inside to the outside. A nozzle is provided at the outer end of each arc-shaped bend, and its inner end is connected to the central fluid tube.

[0009] A fluid conveyor, wherein the material inlet is connected to the fluid conveyor.

[0010] Furthermore, the heat exchanger is a shell-and-tube heat exchanger or a jacketed heat exchanger.

[0011] Furthermore, the fluid center tube is axially provided with 2 to 40 fluid distributors, with each fluid distributor spaced 50 mm to 800 mm apart.

[0012] Furthermore, the heat exchanger has a diameter of 3000mm to 9000mm and a height of 5000mm to 18000mm.

[0013] Furthermore, within each arc bend assembly, the number of arc bends is 1 to 10, and the arc diameter of the arc bends is 100mm to 8500mm.

[0014] Furthermore, the nozzle diameter is 1mm to 10mm, and the diameter of the arc-shaped bend is 3mm to 20mm.

[0015] A method of using a reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by rotational ultra / microgravity and micro-interface as described above includes the following steps:

[0016] (1) The heat exchange fluid inlet and outlet are connected to the device providing cold fluid; the fluid conveyor is connected to each device providing materials, used to convey the materials rosin, hydrogen and catalyst to the material inlet respectively, and enter the fluid center tube of the ultra / microgravity-micro-interface reactor through the material inlet. That is, after the rosin, hydrogen and catalyst enter the first heat exchanger to react, the resulting mixture enters the second heat exchanger through the material outlet of the first heat exchanger. At the same time, hydrogen and catalyst are added to the material inlet of the second heat exchanger, and so on, until the mixture obtained after the reaction in the Nth heat exchanger enters the N+1 heat exchanger and the N+2 heat exchanger through the material outlet from the material inlet of the N+1 heat exchanger and the N+2 heat exchanger respectively. At the same time, hydrogen and catalyst are added to the material inlet of the N+1 heat exchanger and the N+2 heat exchanger respectively;; the material conveyed by the fluid conveyor is determined by the β value, and the specific calculation formula is as follows:

[0017] The centrifugal acceleration is G = Rω 2 (1)

[0018] The Earth's gravitational acceleration is g = 9.81 m / s². 2 (2)

[0019] Ultra / microgravity factor

[0020] Where: G - centrifugal acceleration, m / s² 2 ;

[0021] R - Radius of circular motion, i.e., the radius of the arc of the circular bend, in meters;

[0022] g - Earth's gravitational acceleration, m / s² 2 ;

[0023] ω - angular velocity of circular motion, i.e., the angular velocity of the material in the ultra / microgravity-micro-interface reactor, 1 / s;

[0024] β-microgravity factor;

[0025] N - Rotational speed of circular motion, r / min;

[0026] π — Pi (the mathematical constant of a circle).

[0027] V—Circular motion linear velocity, i.e., the flow velocity of the material in the ultra / microgravity-microinterface reactor, m / s;

[0028] Where R is a known value, and β takes a specific value to make the material in the ultra / microgravity-microinterface reactor be in a microgravity or ultragravity state;

[0029] (2) After the resin, hydrogen and catalyst 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, hydrogen and catalyst are added to the material inlet of the second heat exchanger. This process continues until the mixture obtained after the reaction in the Nth heat exchanger is discharged from the material outlet. Then, it enters the N+1 and N+2 heat exchangers from the material inlets of the N+1 and N+2 heat exchangers respectively. At the same time, hydrogen and catalyst are added to the material inlets of the N+1 and N+2 heat exchangers respectively. The mixture from the Nth heat exchanger and the added hydrogen and catalyst are mixed and reacted simultaneously in the N+1 and N+2 heat exchangers respectively. Similarly, the flow rate of the added hydrogen and catalyst is controlled to conform to the above formula.

[0030] 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 hypergravity field effect is generated, thereby causing heterogeneous reactants to form millimeter- or micrometer-sized droplets and bubbles, which efficiently promotes the interphase mixing and enhances the transfer process of heterogeneous reactants. The value of β is selected by the viscosity, density, temperature and chemical reaction characteristics of the material.

[0031] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0032] This invention utilizes the centrifugal force generated by the self-rotating circular flow of reacting materials within a reaction apparatus to overcome gravity and form a super / microgravity-microinterface field. This causes the heterogeneous reactants to form millimeter- or micrometer-sized droplets and bubbles, efficiently controlling the aggregate scale of the gas-liquid-solid interface from the millimeter-centimeter level to the micrometer level. This effectively promotes interphase mixing and enhances the transport process of heterogeneous reactants. Moreover, the reaction apparatus of this invention does not require specialized mechanical equipment to drive the reactants to generate centrifugal force through high-speed rotation. Because the reactants themselves generate the super / microgravity-microinterface through their own circular rotational flow, the transport process of the reaction system is enhanced. The apparatus is simple in structure, easy to manufacture, convenient to install and maintain, has good sealing performance, and is easy to operate, achieving high-efficiency, low-energy consumption, low-pollution, and low-investment industrial production. Attached Figure Description

[0033] Figure 1 This is a schematic diagram of the unit reaction device for the self-rotating ultra / microgravity-microinterface synergistic enhancement of rosin catalytic hydrogenation according to the present invention.

[0034] Figure 2 This is a top view of the ultra / microgravity-microinterface reactor.

[0035] Figure 3 For heat exchangers, (a) is a shell-and-tube heat exchanger and (b) is a jacketed heat exchanger.

[0036] Figure 4 This is a schematic diagram of the reaction device for the self-rotating ultra / microgravity-microinterface synergistic enhancement of rosin catalytic hydrogenation according to the present invention.

[0037] Figure 5 This is a three-dimensional view of a microgravity / micro-interface reactor.

[0038] 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, 14-fourth heat exchanger, 101-material inlet, 102-material outlet, 103-heat exchange fluid inlet, 104-heat exchange fluid outlet, 301-circular arc bend, 302-nozzle. Detailed Implementation

[0039] The following detailed description, in conjunction with the accompanying drawings, outlines specific embodiments. However, it should be understood that the scope of protection of this invention is not limited to these specific embodiments. Unless otherwise specified, all raw materials and reagents used in the examples are commercially available.

[0040] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0041] Example 1

[0042] Figure 1 and Figure 4 The diagram shows a schematic of a reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by a self-rotating ultra / microgravity-microinterface system according to the present invention. The apparatus includes:

[0043] Heat exchanger 1 has a material inlet 101 at its upper end and a material outlet 102 at its lower end. The side wall of heat exchanger 1 has a heat exchange fluid inlet 103 and a heat exchange fluid outlet 104. There are four or more heat exchangers 1, and the heat exchangers are connected in series and parallel, i.e., a combination of series and parallel connections. 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 inlets 101 of the third heat exchanger 13 and the fourth heat exchanger 14, and so on. The reaction takes place within heat exchanger 1, and the reaction process releases heat. Cold fluid enters and exits heat exchanger 1 to control the reaction temperature.

[0044] Ultra / microgravity-microinterface reactor ( Figure 2 and Figure 5 The ultra / microgravity-microinterface reactor, housed within heat exchanger 1, comprises a fluid center tube 2 and a fluid distributor 3. The fluid center tube 2 is a cylindrical tube open at its upper end, with its upper end connected to the material inlet 101. At least one fluid distributor 3 is axially arranged within the fluid center tube 2. Each fluid distributor 3 comprises at least three arc-shaped bend groups, each comprising at least one arc-shaped bend 301. The arc-shaped bends 301 within the same arc-shaped bend group have the same radius and are radially distributed. When the number of arc-shaped bends 301 within each arc-shaped bend group is ≥2, the arc-shaped bends... The diameter of the arc of tube 301 increases from the inside to the outside. When the material is sprayed out from the nozzles 302 of the arc-shaped tube 301 of varying lengths, the reactants in different areas can be stirred, making the reaction more complete. The outer end of the arc-shaped tube 301 is equipped with nozzles 302, and the inner end of the arc-shaped tube 301 is connected to the fluid center tube 2. The materials are mixed and reacted through the ultra / microgravity-micro-interface reactor. That is, each material enters the fluid center tube 2 to complete the first mixing (during the mixing, the materials also undergo chemical reactions), and then is sprayed into the heat exchanger 1 through the fluid distributor 3 to achieve the second mixing and reaction.

[0045] And fluid conveyor 4, material inlet 101 is connected to fluid conveyor 4, used to convey various materials into the ultra / microgravity-microinterface reactor;

[0046] refer to Figure 1 and Figure 5When there are 3 heat exchangers, 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.

[0047] refer to Figure 1 and Figure 3 Heat exchanger 1 is a shell-and-tube heat exchanger or a jacketed heat exchanger.

[0048] refer to Figure 1 and Figure 2 The fluid center pipe 2 is axially equipped with 2 to 40 fluid distributors 3, and the spacing 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, the more fluid distributors 3 there are. The more fluid distributors 3 there are, the more uniform the mixing and the more thorough the stirring.

[0049] refer to Figure 1 and Figure 3 The diameter of heat exchanger 1 is 3000mm to 9000mm, and the height is 5000mm to 18000mm.

[0050] refer to Figure 2 Within each arc bend assembly, the number of arc bends 301 ranges from 1 to 10, and the arc diameter of the arc bends 301 ranges from 100 mm to 8500 mm.

[0051] Continue to refer to Figure 2 The diameter of nozzle 302 is 1mm to 10mm, and the diameter of arc bend 301 is 3mm to 20mm.

[0052] Example 2

[0053] The operating steps for using the self-rotating ultra / microgravity-microinterface synergistic enhancement reaction device for catalytic hydrogenation of rosin, as described in Example 1, are as follows:

[0054] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device that provides cold fluid for heat exchange. The heat exchanger 1 has a diameter of 9000 mm and a height of 18000 mm. There are 4 heat exchangers 1 connected in series and parallel (e.g. Figure 4The materials rosin, hydrogen, and catalyst are conveyed at a certain speed to the material inlet 101 via the fluid conveyor 4, and then enter the fluid center pipe 2 through the material inlet 101. Each heat exchanger 1 contains a total of 5 arc bend groups, and each arc bend group contains eight arc bends 301. The arc diameter of the first arc bend is 500mm, the second arc bend is 1000mm, the third arc bend is 2500mm, the fourth arc bend is 4000mm, the fifth arc bend is 5000mm, the sixth arc bend is 6000mm, the seventh arc bend is 7000mm, and the eighth arc bend is 8000mm. The nozzle 302 has a diameter of 8 mm, the arc bend 301 has a diameter of 15 mm, and there are 40 fluid distributors 3. After the resin, hydrogen, and catalyst react in the first heat exchanger 11, the resulting mixture is discharged through the material outlet 102 of the first heat exchanger 11 and enters the second heat exchanger 12 through the material inlet 101 for further reaction. The resulting mixture is discharged through the material outlet 102 of the second heat exchanger 12 and enters the third and fourth heat exchangers 13 and 14 through the material inlets 101 for further reaction. The material conveyed by the fluid conveyor 4 has a flow rate V determined by the β value, controlled at 39.74 m / s. The specific calculation formula is shown below.

[0055] The centrifugal acceleration is G = Rω 2 (1)

[0056] The Earth's gravitational acceleration is g = 9.81 m / s². 2 (2)

[0057] Ultra / microgravity factor

[0058] Where: G - centrifugal acceleration, m / s² 2 R - radius of the circular motion, m; g - acceleration due to gravity, m / s² 2 ω - angular velocity of circular motion, 1 / s; β - microgravity factor; N - rotational speed of circular motion, r / min; π - pi; V - linear velocity of circular motion, m / s;

[0059] Specifically, after each material enters the central fluid pipe 2, it is placed in a state of super-heavy / micro-heavy weight, with β ≥ 40. At this time, G ≥ 392.4 m / s 2Because there are eight circular arc bends 301, each with a different arc radius, in order to make the β value meet the above requirements, the arc radius of the largest circular arc bend is used to calculate V, that is, R = 4m, then V = 39.74m / s; because there are different arc radii in the ultra / microgravity-microinterface reactor, the material will be stirred at different positions in the heat exchanger 1 when it is sprayed out, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0060] (2) The resin, hydrogen, and catalyst flowing in from the material inlet 101 are mixed once in the fluid center pipe 2. Since the lower end of the fluid center pipe 2 is closed, the material can only enter the arc bend pipe 301 from the fluid center pipe 2 and be sprayed out through the nozzle 302. Due to the speed given by the fluid conveyor 4, the sprayed material generates centrifugal force, overcomes gravity to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, mixing and reaction occur. The mixture obtained after the reaction in the first heat exchanger 11 enters the second heat exchanger 12 from the material outlet 102. At the same time, hydrogen and catalyst are added to the material inlet 101 of the second heat exchanger 12 (the corresponding material velocity must also satisfy the above equation when adding). The mixture obtained after the reaction in the second heat exchanger 11 enters the second heat exchanger 12 from the material outlet 101. 2. The mixture enters the third heat exchanger 13 and the fourth heat exchanger 14. At the same time, hydrogen and catalyst are added to the material inlet 101 of each of the third heat exchanger 13 and the fourth heat exchanger 14 (the corresponding material rate must satisfy the above equation during addition). The added hydrogen and catalyst, as well as the mixture after reaction from the first heat exchanger 11 / second heat exchanger 12, continue to mix and react in the third heat exchanger 13 and the fourth heat exchanger 14. The product obtained after the reaction is discharged from the material outlet 102. During the reaction, cold fluid enters from the heat exchange fluid inlet 103, exchanges heat with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104. By adopting a series and parallel connection, back mixing in the heat exchanger 1 can be avoided, the driving force of the reaction process can be increased, the reaction time can be extended, and the yield can be increased to achieve mass production.

[0061] Example 3

[0062] The operating steps for using the self-rotating ultra / microgravity-microinterface synergistic enhancement reaction device for catalytic hydrogenation of rosin, as described in Example 1, are as follows:

[0063] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device that provides cold fluid for heat exchange. The heat exchanger 1 has a diameter of 3000 mm and a height of 5000 mm. There are 4 heat exchangers 1 connected in series and parallel (e.g. Figure 4The materials rosin, hydrogen, and catalyst are conveyed at a certain speed to the material inlet 101 via the fluid conveyor 4, and then enter the fluid center pipe 2 through the material inlet 101. Each heat exchanger 1 contains three arc bend groups, and each arc bend group contains four arc bends 301. The arc diameter of the first arc bend is 200mm, the second arc bend is 500mm, the third arc bend is 1000mm, and the fourth arc bend is 2000mm. The nozzle 302 has a diameter of 3mm, and the pipe diameter of the arc bends 301 is 6mm. There are 10 fluid distributors 3. After the resin, hydrogen, and catalyst react in the first heat exchanger 11, the resulting mixture is discharged through the material outlet 102 of the first heat exchanger 11 and enters the second heat exchanger 12 through the material inlet 101 for further reaction. The resulting mixture is discharged through the material outlet 102 of the second heat exchanger 12 and enters the third and fourth heat exchangers 13 and 14 through the material inlets 101 for further reaction. The material conveyed by the fluid conveyor 4 has a flow rate V determined by the β value, controlled at 9.92 m / s. The specific calculation formula is shown below.

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

[0065] The Earth's gravitational acceleration is g = 9.81 m / s². 2 (2)

[0066] Ultra / microgravity factor

[0067] Where: G - centrifugal acceleration, m / s² 2 R - radius of the circular motion, m; g - acceleration due to gravity, m / s² 2 ω - angular velocity of circular motion, 1 / s; β - microgravity factor; N - rotational speed of circular motion, r / min; π - pi; V - linear velocity of circular motion, m / s;

[0068] Specifically, after each material enters the central fluid pipe 2, it is placed in a state of super-heavy / micro-heavy weight, with β ≥ 10. At this time, G ≥ 98.1 m / s 2 Because there are four circular arc bends 301, each with a different arc radius, in order to make the β value meet the above requirements, the arc radius of the largest circular arc bend is used to calculate V, that is, R = 1m, then V = 9.93m / s; because there are different arc radii in the ultra / microgravity-microinterface reactor, the material will be stirred at different positions in the heat exchanger 1 when it is sprayed out, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0069] (2) The resin, hydrogen, and catalyst flowing in from the material inlet 101 are mixed once in the fluid center pipe 2. Since the lower end of the fluid center pipe 2 is closed, the material can only enter the arc bend pipe 301 from the fluid center pipe 2 and be sprayed out through the nozzle 302. Due to the speed given by the fluid conveyor 4, the sprayed material generates centrifugal force, overcomes gravity to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, mixing and reaction occur. The mixture obtained after the reaction in the first heat exchanger 11 enters the second heat exchanger 12 from the material outlet 102. At the same time, hydrogen and catalyst are added to the material inlet 101 of the second heat exchanger 12 (the corresponding material velocity must also satisfy the above equation when adding). The mixture obtained after the reaction in the second heat exchanger 11 enters the second heat exchanger 12 from the material outlet 101. 2. The mixture enters the third heat exchanger 13 and the fourth heat exchanger 14. At the same time, hydrogen and catalyst are added to the material inlet 101 of each of the third heat exchanger 13 and the fourth heat exchanger 14 (the corresponding material rate must satisfy the above equation during addition). The added hydrogen and catalyst, as well as the mixture after reaction from the first heat exchanger 11 / second heat exchanger 12, continue to mix and react in the third heat exchanger 13 and the fourth heat exchanger 14. The product obtained after the reaction is discharged from the material outlet 102. During the reaction, cold fluid enters from the heat exchange fluid inlet 103, exchanges heat with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104. By adopting a series and parallel connection, back mixing in the heat exchanger 1 can be avoided, the driving force of the reaction process can be increased, the reaction time can be extended, and the yield can be increased to achieve mass production.

[0070] Example 4

[0071] The operating steps for using the self-rotating ultra / microgravity-microinterface synergistic enhancement reaction device for catalytic hydrogenation of rosin, as described in Example 1, are as follows:

[0072] (1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are connected to the device that provides cold fluid for heat exchange. The heat exchanger 1 has a diameter of 6000 mm and a height of 12000 mm. There are 4 heat exchangers 1 connected in series and parallel (e.g. Figure 4The materials rosin, hydrogen, and catalyst are conveyed at a certain speed to the material inlet 101 via the fluid conveyor 4, and then enter the fluid center pipe 2 through the material inlet 101. Each heat exchanger 1 contains four arc bend groups, and each arc bend group contains five arc bends 301. The arc diameter of the first arc bend is 900 mm, the second arc bend is 2000 mm, the third arc bend is 3200 mm, the fourth arc bend is 4500 mm, and the fifth arc bend is 5500 mm. The nozzle 302 has a diameter of 5 mm, and the diameter of the arc bends 301 is 10 mm. There are 12 fluid distributors 3. After the resin, hydrogen, and catalyst react in the first heat exchanger 11, the resulting mixture is discharged through the material outlet 102 of the first heat exchanger 11. It then enters the second heat exchanger 12 through the material inlet 101 for further reaction. The resulting mixture is discharged through the material outlet 102 of the second heat exchanger 12. Finally, it enters the third and fourth heat exchangers 13 and 14 through the material inlets 101 for further reaction. The material conveyor 4 transports materials with a flow rate V determined by the β value, controlled at 23.3 m / s. The specific calculation formula is shown below.

[0073] The centrifugal acceleration is G=Rω2 (1)

[0074] The Earth's gravitational acceleration is g = 9.81 m / s². 2 (2)

[0075] Ultra / microgravity factor

[0076] Where: G - centrifugal acceleration, m / s² 2 R - radius of the circular motion, m; g - acceleration due to gravity, m / s² 2 ω - angular velocity of circular motion, 1 / s; β - microgravity factor; N - rotational speed of circular motion, r / min; π - pi; V - linear velocity of circular motion, m / s;

[0077] Specifically, after each material enters the central fluid pipe 2, it is placed in a state of super-heavy / micro-heavy weight, with β≥20. At this time, G≥196.2m / s 2 Because there are five circular arc bends 301, each with a different arc radius, in order to make the β value meet the above requirements, the arc radius of the largest circular arc bend is used to calculate V, that is, R = 2.75m, then V = 23.3m / s; because there are different arc radii in the ultra / microgravity-microinterface reactor, the material will be stirred at different positions in the heat exchanger 1 when it is sprayed out, which increases the uniformity of material mixing, makes the reaction more complete, and reduces the installation of stirring equipment;

[0078] (2) The resin, hydrogen, and catalyst flowing in from the material inlet 101 are mixed once in the fluid center pipe 2. Since the lower end of the fluid center pipe 2 is closed, the material can only enter the arc bend pipe 301 from the fluid center pipe 2 and be sprayed out through the nozzle 302. Due to the speed given by the fluid conveyor 4, the sprayed material generates centrifugal force, overcomes gravity to form a super / microgravity-microinterface field, thereby enhancing the transfer process of the reaction system. During this process, mixing and reaction occur. The mixture obtained after the reaction in the first heat exchanger 11 enters the second heat exchanger 12 from the material outlet 102. At the same time, hydrogen and catalyst are added to the material inlet 101 of the second heat exchanger 12 (the corresponding material velocity must also satisfy the above equation when adding). The mixture obtained after the reaction in the second heat exchanger 11 enters the second heat exchanger 12 from the material outlet 101. 2. The mixture enters the third heat exchanger 13 and the fourth heat exchanger 14. At the same time, hydrogen and catalyst are added to the material inlet 101 of each of the third heat exchanger 13 and the fourth heat exchanger 14 (the corresponding material rate must satisfy the above equation during addition). The added hydrogen and catalyst, as well as the mixture after reaction from the first heat exchanger 11 / second heat exchanger 12, continue to mix and react in the third heat exchanger 13 and the fourth heat exchanger 14. The product obtained after the reaction is discharged from the material outlet 102. During the reaction, cold fluid enters from the heat exchange fluid inlet 103, exchanges heat with the reaction raw materials, and then flows out through the heat exchange fluid outlet 104. By adopting a series and parallel connection, back mixing in the heat exchanger 1 can be avoided, the driving force of the reaction process can be increased, the reaction time can be extended, and the yield can be increased to achieve mass production.

[0079] The foregoing description of specific exemplary embodiments of the invention is for illustrative and explanatory purposes. These descriptions are not intended to limit the invention to the precise forms disclosed, and it will be apparent that many changes and variations can be made in accordance with the foregoing teachings. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application, thereby enabling those skilled in the art to implement and utilize various different exemplary embodiments of the invention, as well as various different choices and variations. The scope of the invention is intended to be defined by the claims and their equivalents.

Claims

1. A reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by self-rotating ultra / microgravity-microinterface, characterized in that: The apparatus for the reaction includes: A heat exchanger has a material inlet and a material outlet at its upper and lower ends, respectively. The side wall of the heat exchanger has a heat exchange fluid inlet and a heat exchange fluid outlet. There are four or more heat exchangers. The heat exchangers are connected in series and parallel, that is, in a series-parallel connection. The material outlet of the first heat exchanger is connected to the material inlet of the second heat exchanger, and so on, until the material outlet of the Nth heat exchanger is connected to the material inlets of the N+1th and N+2th heat exchangers, and so on. A microgravity / micro-gravity micro-interface reactor is disposed within the heat exchanger. The reactor includes a central fluid tube and a fluid distributor. The central fluid tube is a cylindrical tube open at its upper end, and its upper end is connected to the material inlet. At least one fluid distributor is axially arranged on the central fluid tube. Each fluid distributor includes at least three groups of arc-shaped bends, each group comprising at least one arc-shaped bend, and the arc-shaped bends are radially distributed. When the number of arc-shaped bends in each group is ≥2, the arc diameter of the arc-shaped bends increases sequentially from the inside to the outside. A nozzle is provided at the outer end of each arc-shaped bend, and the inner end of each arc-shaped bend is connected to the central fluid tube. A fluid conveyor, wherein the material inlet is connected to the fluid conveyor.

2. The reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by rotational ultra / microgravity-microinterface as described in claim 1, characterized in that: The heat exchanger is a shell-and-tube heat exchanger or a jacketed heat exchanger.

3. The reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by self-rotation, ultra / microgravity, and micro-interface as described in claim 1, characterized in that: The fluid center tube is axially equipped with 2 to 40 fluid distributors, with each fluid distributor spaced 50 mm to 800 mm apart.

4. The reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by self-rotation, ultra / microgravity, and micro-interface as described in claim 1, characterized in that: The heat exchanger has a diameter of 3000 mm to 9000 mm and a height of 5000 mm to 18000 mm.

5. The reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by self-rotation, ultra / microgravity, and micro-interface as described in claim 1, characterized in that: Within each arc bend group, the number of arc bends is 1 to 10, and the arc diameter of the arc bend is 100 mm to 8500 mm.

6. The reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by self-rotation, ultra / microgravity, and micro-interface as described in claim 1, characterized in that: The nozzle diameter is 1 mm to 10 mm, and the diameter of the arc bend is 3 mm to 20 mm.

7. A method of using the reaction apparatus for synergistic enhancement of rosin catalytic hydrogenation by self-rotation ultra / microgravity-microinterface as described in claim 1, characterized in that, Includes the following steps: (1) The heat exchange fluid inlet and outlet are connected to the device that provides cold fluid for heat exchange. The material rosin, hydrogen and catalyst are transported to the fluid center tube by the fluid conveyor. That is, after the rosin, hydrogen and catalyst enter the first heat exchanger and react, the resulting mixture enters the second heat exchanger through the material outlet of the first heat exchanger. At the same time, hydrogen and catalyst are added to the material inlet of the second heat exchanger. And so on, until the mixture is reacted in the Nth heat exchanger, it enters the N+1 heat exchanger and the N+2 heat exchanger through the material outlet from the material inlet of the N+1 heat exchanger and the N+2 heat exchanger. At the same time, hydrogen and catalyst are added to the material inlet of the N+1 heat exchanger and the N+2 heat exchanger respectively. The material conveyed by the fluid conveyor is determined by the value of β, where β is the ultra / microgravity factor. (2) After the resin, hydrogen and catalyst enter the fluid center tube, they are sprayed into the heat exchanger through the arc bend and nozzle to achieve mixing and reaction.

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