CN116159504B - A self-rotating microgravity/hypergravity-microinterface synergistic enhancement reaction device for catalytic hydrogenation of rosin and its operation method - Google Patents
A self-rotating microgravity/hypergravity-microinterface synergistic enhancement reaction device for catalytic hydrogenation of rosin and its operation methodInfo
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- CN116159504B CN116159504B CN202310164247.6A CN202310164247A CN116159504B CN 116159504 B CN116159504 B CN 116159504B CN 202310164247 A CN202310164247 A CN 202310164247A CN 116159504 B CN116159504 B CN 116159504B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/0053—Details of the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09F—NATURAL RESINS; FRENCH POLISH; DRYING-OILS; OIL DRYING AGENTS, i.e. SICCATIVES; TURPENTINE
- C09F1/00—Obtaining purification, or chemical modification of natural resins, e.g. oleo-resins
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- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09F—NATURAL RESINS; FRENCH POLISH; DRYING-OILS; OIL DRYING AGENTS, i.e. SICCATIVES; TURPENTINE
- C09F1/00—Obtaining purification, or chemical modification of natural resins, e.g. oleo-resins
- C09F1/04—Chemical modification, e.g. esterification
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Abstract
The invention discloses a reaction device for self-rotating supergravity-micro interface synergistic reinforced rosin catalytic hydrogenation, which comprises heat exchangers, a supergravity-micro interface reactor and a fluid conveyor, wherein the heat exchangers are connected in series and parallel, namely, are connected in series, combined and parallel, a first heat exchanger material outlet is communicated with a second heat exchanger material inlet, and the like, an Nth heat exchanger material outlet is communicated with an N+1 th and an N+2 th heat exchanger material inlet, the supergravity-micro interface reactor is communicated with the fluid conveyor, and the material inlet is communicated with the fluid conveyor. The invention utilizes the self-rotation circumferential flow of the materials participating in the reaction device to generate centrifugal force so as to overcome the gravity to form an ultra/microgravity-micro interface field, thereby enabling heterogeneous reaction materials to form millimeter-level or micron-level liquid drops and small bubbles, effectively regulating the aggregation scale of a gas-liquid-solid interface from milli-centimeter level to micron level, and effectively promoting the inter-phase mixing and strengthening transfer process of heterogeneous reaction materials.
Description
Technical Field
The invention relates to the technical field of chemical production equipment, in particular to a self-rotating reaction device for catalyzing and hydrogenating rosin by cooperative reinforcement of supergravity/microgravity-microinterface and a use method thereof.
Background
Rosin is a secretion of pine tree called as "petroleum growing on tree", which is one of the biggest biomass grease resources, and rosin and turpentine are obtained by distillation separation of rosin. Rosin is a mixture of thirteen resin acids, a small amount of fatty acids and some neutral substances, and since rosin resin acids contain conjugated double bonds, rosin is easily oxidized by oxygen in the air. The turpentine oil contains alpha-pinene and beta-pinene as main components, and small amount of sesquiterpene, namely longifolene and caryophyllene. The turpentine catalytic hydrogenation comprises hydrogenation reaction of turpentine and rosin, wherein turpentine hydrogenation mainly comprises pinene reaction to generate pinane, the pinane is an important intermediate of fine chemical products such as synthetic drugs, spices and adhesives, and the product obtained by rosin hydrogenation reaction is hydrogenated rosin and has the advantages of good oxidation resistance, small brittleness, high thermal stability, light color and the like. Because of the steric hindrance effect of the abietic acid type resin acid tricyclic phenanthrene skeleton and the high viscosity of the rosin melt, the gas-liquid mass transfer is difficult, the hydrogenation reaction can be carried out under high temperature and high pressure by taking noble metal Pd/C as a catalyst. In the prior art, CN201310673150.4 discloses a device and a method for collecting rosin and preparing hydrocarbon liquid fuel, the device collects the rosin from the inside of plants, the damage to the plants is avoided, the labor productivity of the rosin collection is high, and the rosin with high quality can be obtained. The hydrocarbon liquid fuel can be obtained through the reaction of the hydrogenation reactor, so that the collection and the processing are carried out simultaneously, and the utilization rate and the labor productivity of rosin are improved. CN20110289747. X provides a synthetic process of hydrogenated rosin, which has simple process, short time consumption and mild reaction condition. CN200410078371.8 provides a new method for preparing water-white hydrogenated rosin, which firstly adopts sterilized water quality with low dissolved oxygen to rinse rosin, and removes impurities such as colloid, chlorophyll, trace sugar and protein in rosin. CN01128415.3 discloses a method for preparing hydrogenated rosin by using rosin liquid or 200# solvent oil to dissolve rosin as raw material and using skeleton nickel as catalyst, and is characterized by that it adopts non-noble metal nickel as catalyst, so that its production cost is greatly reduced, and it also has the advantages of mild hydrogenation reaction condition, short technological process, low investment, easy operation and flexible and changeable production. CN98115885.4 discloses a method for preparing rosin or rosin by using solvent as raw material, and said invented method is short in hydrogenation reaction time, long in service life of catalyst and stable in operation. CN93118671.4 is a method for preparing dihydro or tetrahydro gum rosin (hydrogenated rosin for short) by using rosin as raw material, and the method has the advantages of low reaction temperature and pressure, no need of high vacuum distillation, good product quality and low cost, and meets the national conditions.
Said invention uses mechanical equipment and precise instrument to produce supergravity, microinterface, ultrasonic wave, microwave and rotating disk action to intensify chemical transmission process, so that it has the advantages of high energy consumption, equipment investment and operation difficulty.
Disclosure of Invention
In order to solve the technical problems, the invention provides the self-rotating reaction device for the supergravity/microgravity-microinterface synergistic reinforcement of rosin catalytic hydrogenation and the application method thereof, and the centrifugal force generated by the rotating flow of the reaction materials is utilized to overcome the gravity field so as to form the supergravity/microgravity field, thereby realizing the purposes of convenient operation, energy conservation, consumption reduction and equipment investment cost reduction.
In order to achieve the above purpose, the technical scheme provided by the invention is as follows:
The self-rotating super/microgravity-micro interface synergistic strengthening rosin catalytic hydrogenation reaction device comprises:
The heat exchangers are respectively provided with a material inlet and a material outlet at the upper end and the lower end, and the side wall of the heat exchanger is provided with a heat exchange fluid inlet and a heat exchange fluid outlet, wherein the number of the heat exchangers is more than 4, the heat exchangers are connected in series and parallel, namely, the heat exchangers are connected in series and in parallel, the material outlet of the first heat exchanger is communicated with the material inlet of the second heat exchanger, and the like, until the material outlet of the Nth heat exchanger is communicated with the material inlets of the (n+1) th and (n+2) th heat exchangers, and the like;
The super/microgravity-micro interface reactor comprises a fluid central tube and a fluid distributor, wherein the fluid central tube is a cylindrical tube with an opening at the upper end, the upper end of the fluid central tube is communicated with the material inlet, at least 1 fluid distributor is axially arranged on the fluid central tube and comprises at least 3 arc bent tube groups, each arc bent tube group comprises at least 1 arc bent tube, the arc bent tubes are radially distributed, when the number of the arc bent tubes in each arc bent tube group is more than or equal to 2, the arc diameters of the arc bent tubes sequentially increase from inside to outside, a nozzle is arranged at the outer end of each arc bent tube, the inner end of each arc bent tube is communicated with the fluid central tube, and
And the material inlet is communicated with the fluid conveyor.
Further, the heat exchanger is a tube type heat exchanger or a jacket type heat exchanger.
Further, 2-40 fluid distributors are axially arranged on the fluid central tube, and the interval distance of each fluid distributor is 50-800 mm.
Further, the diameter of the heat exchanger is 3000 mm-9000 mm, and the height is 5000 mm-18000 mm.
Further, in each arc bending tube group, the number of the arc bending tubes is 1-10, and the arc diameter of each arc bending tube is 100-8500 mm.
Further, the diameter of the nozzle is 1 mm-10 mm, and the diameter of the pipe diameter of the arc bent pipe is 3 mm-20 mm.
The application method of the self-rotating super/microgravity-micro interface synergistic reinforced rosin catalytic hydrogenation reaction device comprises the following steps:
(1) The fluid conveyor is communicated with each device for providing materials, and is used for conveying materials rosin, hydrogen and catalysts into a fluid central tube of the ultra/microgravity-micro interface reactor through the material inlet, namely, after the rosin, the hydrogen and the catalysts enter the first heat exchanger for reaction, the mixture obtained after the reaction enters the second heat exchanger through a material outlet of the first heat exchanger, meanwhile, the hydrogen and the catalysts are added into the material inlet of the second heat exchanger in a supplementing way, and the mixture obtained after the reaction in the N heat exchanger enters the N+1 heat exchanger and the N+2 heat exchanger through a material outlet from a material inlet of the N+1 heat exchanger and a material inlet of the N+2 heat exchanger, and meanwhile, the hydrogen and the catalysts are added into the material inlet of the N+1 heat exchanger and the material inlet of the N+2 heat exchanger respectively:
Centrifugal acceleration g=rω 2 (1)
The earth gravity acceleration is g=9.81 m/s 2 (2)
Supergravity/microgravity factor
Wherein G-centrifugal acceleration, m/s 2;
R-circular motion radius, namely the arc radius of the arc bent pipe, m;
g-earth gravitational acceleration, m/s 2;
Omega-circular motion angular velocity, namely angular velocity of materials in the ultra/microgravity-micro interface reactor, 1/s;
beta-supergravity factor;
N-circular motion rotating speed, r/min;
Pi-circumference ratio;
V-circular motion linear velocity, namely the flow velocity of the material in the ultra/microgravity-micro interface reactor, m/s;
wherein R is a known value, beta is a specific value, so that the material is in a micro-weight or overweight state in the ultra/micro-gravity-micro-interface reactor;
(2) After rosin, hydrogen and a catalyst enter a fluid central tube, the rosin, the hydrogen and the catalyst are sprayed in a heat exchanger through an arc bent tube and a nozzle to realize mixing and reaction, the mixture obtained after the reaction of the first heat exchanger enters a second heat exchanger from a material outlet, meanwhile, the hydrogen and the catalyst are added in a material inlet of the second heat exchanger in a complementary manner, and the mixture obtained after the reaction in the nth heat exchanger is discharged through the material outlet, then enters the nth heat exchanger and the nth heat exchanger from a material inlet of the nth heat exchanger and the nth heat exchanger, and meanwhile, the hydrogen and the catalyst are added in a material inlet of the nth heat exchanger and a material inlet of the nth heat exchanger respectively, the mixture obtained from the nth heat exchanger and the added hydrogen and the catalyst are mixed and reacted in the nth heat exchanger respectively, and the flow rates of the added hydrogen and the catalyst are controlled to meet the formula.
When the centrifugal force acceleration G is 1-50 times of the earth gravity acceleration G, namely beta=1-50, a micro gravity field effect is generated, and when the centrifugal force acceleration G is greater than 50 times of the earth gravity acceleration G, namely beta >50, a super gravity field effect is generated, so that millimeter-level or micron-level small liquid drops and small bubbles are formed by heterogeneous reaction materials, the inter-phase mixing and strengthening transfer process of the heterogeneous reaction materials is efficiently promoted, and the beta value is selected according to the viscosity, density, temperature and chemical reaction characteristics of the materials.
Compared with the prior art, the invention has the beneficial effects that:
The invention uses the self-rotation circumferential flow of the materials participating in the reaction device to generate centrifugal force so as to overcome the gravity to form an ultra/microgravity-micro interface field, thereby leading heterogeneous reaction materials to form millimeter-level or micron-level small liquid drops and small bubbles, effectively regulating the aggregation scale of a gas-liquid-solid interface from milli-centimeter level to micrometer level, and effectively promoting the inter-phase mixing and strengthening transmission process of the heterogeneous reaction materials.
Drawings
FIG. 1 is a schematic diagram of a unit reaction apparatus for self-rotating supergravity/microgravity-microinterface collaborative strengthening rosin catalytic hydrogenation.
FIG. 2 is a top view of an ultra/microgravity-micro interface reactor.
Fig. 3 shows a heat exchanger, wherein (a) is a tube type heat exchanger and (b) is a jacket type heat exchanger.
FIG. 4 is a schematic diagram of a reaction apparatus for catalytic hydrogenation of self-rotating supergravity/microgravity-microinterface collaborative reinforced rosin.
FIG. 5 is a perspective view of an ultra/microgravity-micro interface reactor.
The heat exchanger comprises a 1-heat exchanger, a 2-fluid central tube, a 3-fluid distributor, a 4-fluid conveyor, a 11-first heat exchanger, a 12-second heat exchanger, a 13-third heat exchanger, a 14-fourth heat exchanger, a 101-material inlet, a 102-material outlet, a 103-heat exchange fluid inlet, a 104-heat exchange fluid outlet, a 301-circular arc bent tube and a 302-nozzle.
Detailed Description
The following detailed description, in conjunction with the accompanying drawings, describes in detail, but it is to be understood that the scope of the invention is not limited to the specific embodiments. The raw materials and reagents used in the examples were commercially available unless otherwise specified.
Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations thereof such as "comprises" or "comprising", etc. will be understood to include the stated element or component without excluding other elements or components.
Example 1
FIGS. 1 and 4 show a schematic structural diagram of a reaction apparatus for catalytic hydrogenation of self-rotating supergravity/microgravity-microinterface collaborative reinforced rosin, which comprises:
The heat exchanger 1 is provided with a material inlet 101 at the upper end and a material outlet 102 at the lower end, and the side wall of the heat exchanger 1 is provided with a heat exchange fluid inlet 103 and a heat exchange fluid outlet 104, wherein the number of the heat exchangers 1 is more than 4, the heat exchangers are connected in series and in parallel, namely, the first heat exchanger 11 is connected in series and in parallel, the material outlet 102 of the first heat exchanger 11 is communicated with the material inlet 101 of the second heat exchanger 12, the material outlet 102 of the second heat exchanger 12 is communicated with the material inlets 101 of the third heat exchanger 13 and the fourth heat exchanger 14, and the like;
The super/microgravity-micro interface reactor (figures 2 and 5) is arranged in the heat exchanger 1, the super/microgravity-micro interface reactor comprises a fluid central tube 2 and a fluid distributor 3, the fluid central tube 2 is a cylindrical tube with an opening at the upper end, the upper end of the fluid central tube 2 is communicated with a material inlet 101, at least 1 fluid distributor 3 is axially arranged on the fluid central tube 2, the fluid distributor 3 comprises at least 3 circular arc bent tube groups, each circular arc bent tube group comprises at least 1 circular arc bent tube 301, the circular arc bent tubes 301 in the same circular arc bent tube group have the same radius, the circular arc bent tubes 301 are radially distributed, when the number of the circular arc bent tubes 301 in each circular arc bent tube group is equal to or more than 2, the circular arc diameters of the circular arc bent tubes 301 are sequentially increased from inside to outside, so that when materials are sprayed out from nozzles 302 of the circular arc bent tubes 301 with different lengths, the reaction materials in different areas can be stirred, the outer ends of the circular arc bent tubes 301 are provided with nozzles 302, the inner ends of the circular arc bent tubes 301 are communicated with the fluid central tube 2, the materials are mixed through the super/microgravity-micro interface reactor, namely the materials are mixed in the fluid central tube 2, and the mixed materials are mixed in the fluid central tube 1, and the mixed fluid is mixed in the secondary reactor (the secondary heat exchanger is mixed by the secondary fluid 1);
And a fluid conveyor 4, a material inlet 101 in communication with the fluid conveyor 4 for conveying each material into the ultra/microgravity-microinterface reactor;
referring to fig. 1 and 5, when the number of heat exchangers 1 is 3, the material outlet 102 of the first heat exchanger 11 is communicated with the material inlet 101 of the second heat exchanger 12, and the material outlet 102 of the second heat exchanger 12 is communicated with the material inlet 101 of the third heat exchanger 13.
Referring to fig. 1 and 3, the heat exchanger 1 is a tube type heat exchanger or a jacket type heat exchanger.
Referring to fig. 1 and 2,2 to 40 fluid distributors 3 are axially arranged on a fluid central tube 2, the interval distance of each fluid distributor 3 is 50mm to 800mm, the number of the fluid distributors 3 depends on the size of a heat exchanger 1, the larger the heat exchanger 1 is, the more the number of the fluid distributors 3 is, the more uniform mixing is achieved, and stirring is more sufficient.
Referring to fig. 1 and 3, the heat exchanger 1 has a diameter of 3000mm to 9000mm and a height of 5000mm to 18000mm.
Referring to fig. 2, in each arc tube group, the number of arc tube bends 301 is 1 to 10, and the arc diameter of the arc tube bends 301 is 100mm to 8500mm.
With continued reference to FIG. 2, the diameter of the nozzle 302 is 1mm to 10mm, and the pipe diameter of the circular arc elbow 301 is 3mm to 20mm.
Example 2
The method of using the self-rotating super/microgravity-micro interface collaborative enhanced rosin catalytic hydrogenation reaction device of example 1 comprises the following steps:
(1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are communicated with a device for providing cold fluid and used for heat exchange, the diameter of each heat exchanger 1 is 9000mm, the height of each heat exchanger is 18000mm, 4 heat exchangers 1 are connected in series and parallel (as shown in fig. 4), material rosin, hydrogen and a catalyst are respectively conveyed to the material inlet 101 through the fluid conveyor 4 at a certain speed, the material inlet 101 enters the fluid central tube 2, 5 arc bending tubes in each heat exchanger 1 are provided, eight arc bending tubes 301 are arranged in each arc bending tube group, the diameter of a first arc bending tube is 500mm, the diameter of a second arc bending tube is 1000mm, the diameter of a third arc bending tube is 2500mm, the diameter of a fourth arc bending tube is 4000mm, the diameter of a fifth arc bending tube is 5000mm, the diameter of a sixth arc bending tube is 6000mm, the diameter of a seventh arc bending tube is 7000mm, the diameter of an eighth arc bending tube is 8000mm, the diameter of a nozzle 302 is 8mm, the diameter of the arc bending tube is 15mm, and the diameter of the fluid distributor is 3.40; after rosin, hydrogen and a catalyst enter the first heat exchanger 11 for reaction, the mixture obtained after the reaction is discharged through a material outlet 102 of the first heat exchanger 11, enters the second heat exchanger 12 for reaction through a material inlet 101 of the second heat exchanger 12, and is discharged through a material outlet 102 of the second heat exchanger 12, and enters the third heat exchanger 13 and the fourth heat exchanger 14 for respective reaction from a material inlet 101 of the third heat exchanger 13 and the fourth heat exchanger 14, wherein the material flow rate V of the material conveyed by the fluid conveyor 4 is determined by the value of beta, the material flow rate is controlled to be 39.74m/s, and the specific calculation formula is shown as follows:
Centrifugal acceleration g=rω 2 (1)
The earth gravity acceleration is g=9.81 m/s 2 (2)
Supergravity/microgravity factor
Wherein the formula is G-centrifugal acceleration, m/s 2, R-circular motion radius, m, G-earth gravity acceleration, m/s 2, omega-circular motion angular velocity, 1/s, beta-supergravity/microgravity factor, N-circular motion rotating speed, R/min, pi-circular rate, V-circular motion linear velocity and m/s;
Specifically, after entering the fluid central tube 2, each material is in an ultra/micro-heavy state, beta is more than or equal to 40, G is more than or equal to 392.4m/s 2 at the moment, because eight arc elbows 301 are arranged, the arc radius of each arc elbows is different, in order to enable the beta value to meet the requirements, the arc radius of the largest arc elbows is adopted to calculate V, namely R=4m, then V=39.74 m/s;
(2) The rosin, hydrogen and catalyst flowing in from the material inlet 101 are mixed once in the fluid central tube 2, the material can only enter the circular arc bent tube 301 from the fluid central tube 2 because the lower end of the fluid central tube 2 is closed and is sprayed out through the nozzle 302, the sprayed material generates centrifugal force to overcome gravity to form an ultra/microgravity-micro interface field due to the speed given by the fluid conveyor 4, the transmission process of a reaction system is intensified, the mixture is mixed and reacted in the process, the mixture obtained after the first heat exchanger 11 is reacted enters the second heat exchanger 12 from the material outlet 102, meanwhile, the hydrogen and the catalyst are added in the material inlet 101 of the second heat exchanger 12 (the corresponding material speed is also satisfied in the process of adding), the mixture obtained after the second heat exchanger 11 is reacted enters the third heat exchanger 13 and the fourth heat exchanger 14 from the material outlet 102, and the hydrogen and the catalyst are added in the process of adding in the material inlet 101 of the third heat exchanger 13 and the fourth heat exchanger 14 (the corresponding speed is satisfied in the process of adding), the added hydrogen and the catalyst are also satisfied in the process of supplementing the process of adding in the process of the material, and the mixture obtained after the second heat exchanger 11 is discharged from the material outlet 102 and the mixture obtained after the second heat exchanger 12 is discharged from the second heat exchanger 14 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 flows out through the heat exchange fluid outlet 104, and adopts a series connection and parallel connection mode, thereby not only avoiding the back mixing phenomenon in the heat exchanger 1, improving the driving force of the reaction process, prolonging the reaction time, but also improving the yield, realizing quantitative production.
Example 3
The method of using the self-rotating super/microgravity-micro interface collaborative enhanced rosin catalytic hydrogenation reaction device of example 1 comprises the following steps:
(1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are communicated with a device for providing cold fluid and are used for heat exchange, the diameter of each heat exchanger 1 is 3000mm, the height of each heat exchanger is 5000mm, 4 heat exchangers 1 are connected in series and parallel (as shown in figure 4), material rosin, hydrogen and a catalyst are respectively conveyed to the material inlet 101 through the fluid conveyor 4 at a certain speed and enter the fluid central tube 2 through the material inlet 101, 3 arc bent tube groups in each heat exchanger 1 are provided, four arc bent tubes 301 are arranged in each arc bent tube group, the arc diameter of the first arc bent tube is 200mm, the arc diameter of the second arc bent tube is 500mm, the arc diameter of the third arc bent tube is 1000mm, the arc diameter of the fourth arc bent tube is 2000mm, the diameter of the nozzle 302 is 3mm, the diameter of the arc bent tube 301 is 6mm, and 10 fluid distributor 3 are provided; after rosin, hydrogen and a catalyst enter the first heat exchanger 11 for reaction, the mixture obtained after the reaction is discharged through a material outlet 102 of the first heat exchanger 11, enters the second heat exchanger 12 for reaction through a material inlet 101 of the second heat exchanger 12, and is discharged through a material outlet 102 of the second heat exchanger 12, and enters the third heat exchanger 13 and the fourth heat exchanger 14 for respective reaction from a material inlet 101 of the third heat exchanger 13 and the fourth heat exchanger 14, wherein the material flow rate V of the material conveyed by the fluid conveyor 4 is determined by the value of beta, the material flow rate is controlled to be 9.92m/s, and the specific calculation formula is shown as follows:
Centrifugal acceleration g=rω 2 (1)
The earth gravity acceleration is g=9.81 m/s 2 (2)
Supergravity/microgravity factor
Wherein the formula is G-centrifugal acceleration, m/s 2, R-circular motion radius, m, G-earth gravity acceleration, m/s 2, omega-circular motion angular velocity, 1/s, beta-supergravity/microgravity factor, N-circular motion rotating speed, R/min, pi-circumference ratio, V-circular motion linear velocity and m/s;
Specifically, after entering the fluid central tube 2, each material is in an ultra/micro-heavy state, beta is more than or equal to 10, at the moment, G is more than or equal to 98.1m/s 2, because four arc elbows 301 are arranged, the arc radius of each arc elbows is different, in order to enable the beta value to meet the requirements, the arc radius of the largest arc elbows is adopted to calculate V, namely R=1m, and V=9.93 m/s;
(2) The rosin, hydrogen and catalyst flowing in from the material inlet 101 are mixed once in the fluid central tube 2, the material can only enter the circular arc bent tube 301 from the fluid central tube 2 because the lower end of the fluid central tube 2 is closed and is sprayed out through the nozzle 302, the sprayed material generates centrifugal force to overcome gravity to form an ultra/microgravity-micro interface field due to the speed given by the fluid conveyor 4, the transmission process of a reaction system is intensified, the mixture is mixed and reacted in the process, the mixture obtained after the first heat exchanger 11 is reacted enters the second heat exchanger 12 from the material outlet 102, meanwhile, the hydrogen and the catalyst are added in the material inlet 101 of the second heat exchanger 12 (the corresponding material speed is also satisfied in the process of adding), the mixture obtained after the second heat exchanger 11 is reacted enters the third heat exchanger 13 and the fourth heat exchanger 14 from the material outlet 102, and the hydrogen and the catalyst are added in the process of adding in the material inlet 101 of the third heat exchanger 13 and the fourth heat exchanger 14 (the corresponding speed is satisfied in the process of adding), the added hydrogen and the catalyst are also satisfied in the process of supplementing the process of adding in the process of the material, and the mixture obtained after the second heat exchanger 11 is discharged from the material outlet 102 and the mixture obtained after the second heat exchanger 12 is discharged from the second heat exchanger 14 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 flows out through the heat exchange fluid outlet 104, and adopts a series connection and parallel connection mode, thereby not only avoiding the back mixing phenomenon in the heat exchanger 1, improving the driving force of the reaction process, prolonging the reaction time, but also improving the yield, realizing quantitative production.
Example 4
The method of using the self-rotating super/microgravity-micro interface collaborative enhanced rosin catalytic hydrogenation reaction device of example 1 comprises the following steps:
(1) The heat exchange fluid inlet 103 and the heat exchange fluid outlet 104 are communicated with a device for providing cold fluid and are used for heat exchange, the diameter of each heat exchanger 1 is 6000mm, the height of each heat exchanger is 12000mm, 4 heat exchangers 1 are connected in series and parallel (as shown in fig. 4), material rosin, hydrogen and a catalyst are respectively conveyed to the material inlet 101 through the fluid conveyor 4 at a certain speed, the material inlet 101 enters the fluid central tube 2,4 arc bending tubes in each heat exchanger 1 are provided, five arc bending tubes 301 are arranged in each arc bending tube group, the arc diameter of the first arc bending tube is 900mm, the arc diameter of the second arc bending tube is 2000mm, the arc diameter of the third arc bending tube is 3200mm, the arc diameter of the fourth arc bending tube is 4500mm, the arc diameter of the fifth arc bending tube is 5500mm, the diameter of the nozzle 302 is 5mm, the pipe diameter of the arc bending tube 301 is 10mm, and the fluid distributor 3 is 12; after rosin, hydrogen and a catalyst enter the first heat exchanger 11 for reaction, the mixture obtained after the reaction is discharged through a material outlet 102 of the first heat exchanger 11, enters the second heat exchanger 12 for reaction through a material inlet 101 of the second heat exchanger 12, the mixture obtained after the reaction of the second heat exchanger 12 is discharged through a material outlet 102 of the second heat exchanger 12, enters the third heat exchanger 13 and the fourth heat exchanger 14 for respective reaction from a material inlet 101 of the third heat exchanger 13 and the fourth heat exchanger 14, wherein the material flow rate V of the material conveyed by the fluid conveyor 4 is determined by the beta value, the material flow rate is controlled to be 23.3m/s, and the specific calculation formula is shown as follows:
centrifugal acceleration g=rω2 (1)
The earth gravity acceleration is g=9.81 m/s 2 (2)
Supergravity/microgravity factor
Wherein the formula is G-centrifugal acceleration, m/s 2, R-circular motion radius, m, G-earth gravity acceleration, m/s 2, omega-circular motion angular velocity, 1/s, beta-supergravity/microgravity factor, N-circular motion rotating speed, R/min, pi-circular rate, V-circular motion linear velocity and m/s;
specifically, after entering the fluid central tube 2, each material is in an ultra/micro-heavy state, beta is more than or equal to 20, G is more than or equal to 196.2m/s 2 at the moment, because five arc elbows 301 are arranged, the arc radius of each arc elbows is different, in order to enable the beta value to meet the requirements, the arc radius of the largest arc elbows is adopted to calculate V, namely R=2.75m, V=23.3 m/s, and because the ultra/micro-gravity-micro interface reactor is provided with the arc radii of different arc elbows, the material can be stirred at different positions of the heat exchanger 1 when being sprayed out, so that the mixing uniformity degree of the material is increased, the reaction is more sufficient, and the installation of stirring equipment is reduced;
(2) The rosin, hydrogen and catalyst flowing in from the material inlet 101 are mixed once in the fluid central tube 2, the material can only enter the circular arc bent tube 301 from the fluid central tube 2 because the lower end of the fluid central tube 2 is closed and is sprayed out through the nozzle 302, the sprayed material generates centrifugal force to overcome gravity to form an ultra/microgravity-micro interface field due to the speed given by the fluid conveyor 4, the transmission process of a reaction system is intensified, the mixture is mixed and reacted in the process, the mixture obtained after the first heat exchanger 11 is reacted enters the second heat exchanger 12 from the material outlet 102, meanwhile, the hydrogen and the catalyst are added in the material inlet 101 of the second heat exchanger 12 (the corresponding material speed is also satisfied in the process of adding), the mixture obtained after the second heat exchanger 11 is reacted enters the third heat exchanger 13 and the fourth heat exchanger 14 from the material outlet 102, and the hydrogen and the catalyst are added in the process of adding in the material inlet 101 of the third heat exchanger 13 and the fourth heat exchanger 14 (the corresponding speed is satisfied in the process of adding), the added hydrogen and the catalyst are also satisfied in the process of supplementing the process of adding in the process of the material, and the mixture obtained after the second heat exchanger 11 is discharged from the material outlet 102 and the mixture obtained after the second heat exchanger 12 is discharged from the second heat exchanger 14 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 flows out through the heat exchange fluid outlet 104, and adopts a series connection and parallel connection mode, thereby not only avoiding the back mixing phenomenon in the heat exchanger 1, improving the driving force of the reaction process, prolonging the reaction time, but also improving the yield, realizing quantitative production.
The foregoing descriptions of specific exemplary embodiments of the present invention are presented for purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain the specific principles of the invention and its practical application to thereby enable one skilled in the art to make and utilize the invention in various exemplary embodiments and with various modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims and their equivalents.
Claims (7)
1. A reaction device for catalyzing hydrogenation of rosin by self-rotation super/microgravity-micro interface cooperative reinforcement is characterized in that the reaction device comprises:
The heat exchangers are connected in series and in parallel, namely in a series-combined parallel connection mode, the material outlet of the first heat exchanger is communicated with the material inlet of the second heat exchanger, and the like, and the material outlet of the nth heat exchanger is communicated with the material inlets of the (n+1) th and (n+2) th heat exchangers, and the like;
The super/microgravity-micro interface reactor comprises a fluid central tube and a fluid distributor, wherein the fluid central tube is a cylindrical tube with an opening at the upper end, the upper end of the fluid central tube is communicated with the material inlet, at least 1 fluid distributor is axially arranged on the fluid central tube and comprises at least 3 arc bent tube groups, each arc bent tube group comprises at least 1 arc bent tube, the arc bent tubes are radially distributed, when the number of the arc bent tubes in each arc bent tube group is more than or equal to 2, the arc diameters of the arc bent tubes sequentially increase from inside to outside, a nozzle is arranged at the outer end of each arc bent tube, the inner ends of the arc bent tubes are communicated with the fluid central tube, and
And the material inlet is communicated with the fluid conveyor.
2. The reaction device for catalyzing and hydrogenating the rosin by self-rotating super/microgravity-micro interface collaborative strengthening of the reaction device is characterized in that the heat exchanger is a shell and tube heat exchanger or a jacket heat exchanger.
3. The reaction device for catalyzing and hydrogenating the self-rotating supergravity/microgravity-microinterface collaborative strengthening rosin is characterized in that 2-40 fluid distributors are axially arranged on the fluid central tube, and the interval distance of each fluid distributor is 50-800 mm.
4. The reaction device for catalyzing and hydrogenating the self-rotating supergravity/microgravity-microinterface collaborative strengthening rosin is characterized in that the diameter of the heat exchanger is 3000-9000 mm, and the height of the heat exchanger is 5000-18000 mm.
5. The reaction device for catalyzing and hydrogenating the self-rotating supergravity/microgravity-microinterface collaborative strengthening rosin is characterized in that the number of the arc bent pipes in each arc bent pipe group is 1-10, and the arc diameter of the arc bent pipes is 100-8500 mm.
6. The reaction device for catalyzing and hydrogenating the self-rotating supergravity/microgravity-microinterface collaborative strengthening rosin is characterized in that the diameter of the nozzle is 1-10 mm, and the pipe diameter of the arc bent pipe is 3-20 mm.
7. A method of using the self-rotating super/microgravity-microinterface synergistically enhanced rosin catalytic hydrogenation reaction apparatus of claim 1, comprising the steps of:
(1) The heat exchange fluid inlet and the heat exchange fluid outlet are communicated with a device for providing cold fluid and are used for heat exchange, material rosin, hydrogen and a catalyst are conveyed into a fluid central tube through a fluid conveyor, namely, after the rosin, the hydrogen and the catalyst enter a first heat exchanger for reaction, the mixture obtained after the reaction enters a second heat exchanger through a material outlet of the first heat exchanger, meanwhile, hydrogen and the catalyst are added into a material inlet of the second heat exchanger, and the mixture obtained after the reaction in an nth heat exchanger enters the n+1 heat exchanger and the n+2 heat exchanger through a material outlet from a material inlet of the n+1 heat exchanger and a material inlet of the n+2 heat exchanger, and meanwhile, hydrogen and the catalyst are respectively added into a material inlet of the n+1 heat exchanger and a material inlet of the n+2 heat exchanger;
(2) After rosin, hydrogen and a catalyst enter a fluid central tube, the rosin, the hydrogen and the catalyst are sprayed into a heat exchanger through an arc bent tube and a nozzle, so that mixing and reaction are realized.
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| CN116037031A (en) * | 2023-02-24 | 2023-05-02 | 广西大学 | A micro/hypergravity-micro-interface spray spin-rotation reaction device for strengthening heavy turpentine/resin oil catalytic hydrogenation and its application method |
| CN116196860A (en) * | 2023-02-24 | 2023-06-02 | 广西大学 | Device for self-rotation super/microgravity-micro interface collaborative reinforcement of carbon tetraalkylation reaction and application method thereof |
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| CN106905855A (en) * | 2017-03-29 | 2017-06-30 | 南宁市青秀区嘉利林化有限公司 | The method that hydrogenated rosin is prepared from rosin |
| CN111359556A (en) * | 2019-03-15 | 2020-07-03 | 南京延长反应技术研究院有限公司 | A Micro-Interface Enhanced Hydrogenation Reaction System |
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| CN116037031A (en) * | 2023-02-24 | 2023-05-02 | 广西大学 | A micro/hypergravity-micro-interface spray spin-rotation reaction device for strengthening heavy turpentine/resin oil catalytic hydrogenation and its application method |
| CN116196860A (en) * | 2023-02-24 | 2023-06-02 | 广西大学 | Device for self-rotation super/microgravity-micro interface collaborative reinforcement of carbon tetraalkylation reaction and application method thereof |
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