CN215389283U - Tower type continuous flow reactor - Google Patents
Tower type continuous flow reactor Download PDFInfo
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- CN215389283U CN215389283U CN202121622795.1U CN202121622795U CN215389283U CN 215389283 U CN215389283 U CN 215389283U CN 202121622795 U CN202121622795 U CN 202121622795U CN 215389283 U CN215389283 U CN 215389283U
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Abstract
The application discloses a tower type continuous flow reactor, wherein a motor is arranged at the top of the reactor and is connected with a stirring shaft; the reactor is divided into a plurality of reaction chambers by partition plates; be equipped with a plurality of liter liquid holes and a shaft hole on the baffle, the (mixing) shaft extends to the reactor bottom through the shaft hole, and liquid passes through the liter liquid hole on the baffle, and from the bottom up passes through every reaction chamber of reactor in proper order and reacts. In the reactor, a layer of stirring blades is arranged in each reaction chamber, all the stirring blades are connected to the same stirring shaft, and the stirring shaft is driven by a motor to rotate so as to be driven by the stirring shaft to rotate; and a coil heat exchanger is arranged in each reaction chamber, and the reaction temperature in each reaction chamber can be independently controlled. The device has the advantages of small occupied area, low cost and convenience in regulation and control, and can be applied to continuous production occasions of various reactions.
Description
Technical Field
The application relates to the field of chemical equipment, in particular to a tower type continuous flow reactor.
Background
In the actual production process of chemical industry, the continuous flow reactor can continuously carry out the reaction, and the production process is uninterrupted. However, the traditional stirring reactor has the problems of uneven stirring, insufficient reaction, poor material fluidity, dead reaction zone and the like.
Aiming at the problems, Li Fu Qing and the like disclose a stirring multi-section horizontal reactor (application number: 201720822643.3), a plurality of upper baffle plates and lower baffle plates are arranged in the reactor, the baffle plates divide the reactor into a plurality of reaction sections, a stirrer is arranged in each reaction section, the reaction can be carried out under the conditions of normal pressure and high pressure, and the back mixing problem which is easy to occur in the traditional reactor can not occur; the Lien end discloses a hydrometallurgy horizontal multistage reaction kettle (application number: 201520198485. X), a guide plate group is arranged between two stirring devices, the guide plate groups are uniformly distributed, the reaction in the whole kettle is uniform, and the reaction effect is better; liupeng and the like disclose a multistage horizontal stirring airlift reactor (application number: 201711243677.8), a plurality of partition plates are longitudinally arranged in the reactor, a liquid phase channel is arranged between a reaction chamber and the reaction chamber, the top of the reactor is provided with an exhaust hole, and the middle of the reactor is provided with a stirring device, so that gas in the reactor can be distributed more uniformly, and the operation is safer and more reliable; the french et al discloses a multistage stirred reactor (application No. 201580021196.5) with reduced back-mixing, provided with a plurality of stirring chambers and at least one stirring element, having a large specific heat exchange surface by controlling the opening inside the reactor with a brake lever, and being applicable to various situations such as chemical reactions and extractions. However, the existing reactor still has the problems of large occupied area, complex operation and the like.
Disclosure of Invention
In view of the above technical problems in the prior art, the present application aims to provide a tower type continuous flow reactor, which can be applied to a chemical reaction process for continuously preparing chemical products by using multilayer continuous stirring.
The tower type continuous flow reactor is of a tower structure, and comprises a motor and a speed reducer arranged at the top of the reactor, wherein the motor is connected with a stirring shaft through the speed reducer, and the stirring shaft is provided with a plurality of stirring blades. The stirring shaft is mechanically sealed with the top of the reactor, and the bottom end of the stirring shaft is arranged on the bottom wall of the reactor through a bearing.
The tower type continuous flow reactor is characterized in that the reactor is of a tower type structure, a plurality of clapboards are arranged in the reactor at intervals from bottom to top, the clapboards divide the reactor into a plurality of reaction chambers, each clapboard is provided with a plurality of liquid lifting holes and a shaft hole for penetrating through a stirring shaft, and the shaft holes on the clapboards are positioned on the same vertical line; the lower end of the stirring shaft extends into the reactor from the top of the reactor and extends to the bottom of the reactor through the shaft hole on the partition plate; in the reactor, at least one layer of stirring blade is fixedly arranged on a stirring shaft in each reaction chamber; in the reactor, the bottom of the reaction chamber at the bottom is provided with a feed inlet, the upper part of the reaction chamber at the top is provided with a discharge outlet, when reaction liquid is introduced into the reactor from the feed inlet, the reaction liquid can pass through liquid lifting holes on the partition plate, and the reaction liquid sequentially passes through each reaction chamber of the reactor from bottom to top to react, and finally, reaction products flow out from the discharge outlet.
The tower type continuous flow reactor is characterized in that the aperture of liquid lifting holes on the partition plate is 3-40 mm, and the number of the liquid lifting holes on the partition plate is 1-10; the total opening area of the liquid lifting holes on the partition plate is 5-50% of the area of the partition plate.
The tower type continuous flow reactor is characterized in that the height of a liquid lifting pipe on the partition plate is 2-20 cm.
The tower type continuous flow reactor is characterized in that the ratio of the outer diameter of the stirring blade to the inner diameter of the reactor is 0.1-0.9: 1.
The tower type continuous flow reactor is characterized in that the number of reaction chambers formed by separating the reactor by a partition plate is 3-30.
The tower type continuous flow reactor is characterized in that each reaction chamber is provided with a temperature measuring instrument, and the uppermost reaction chamber is provided with a pressure gauge.
In the reactor in the present application, further, the upper part of each reaction chamber is provided with a sampling port, and the sampling port is provided with a valve, so that the reaction progress in each reaction chamber is sampled and analyzed.
In the reactor in this application, the reactor is separated into a plurality of reacting chamber by the polylith baffle, all cooperates on the liquid lift hole of every baffle and installs the stalk to install the check valve on the stalk, make liquid only to flow toward one direction. In addition, in the reactor, each reaction chamber is internally provided with a coil heat exchanger, and a refrigerant medium or a heating medium is respectively introduced into the coil heat exchanger in each reaction chamber so as to independently control the reaction temperature in each reaction chamber of the reactor; wherein, the inlet end and the outlet end of the coil heat exchanger both penetrate out from the side wall of the reactor.
Therefore, in the reactor structure of the application, the problem of back mixing between two adjacent reaction chambers hardly exists, and the reaction process can be effectively accelerated in the continuous reaction process. In the continuous reaction process, the reaction temperature in each reaction chamber can be independently controlled.
The tower type continuous flow reactor is applied to the production of biodiesel through ester exchange reaction, and is characterized in that an alkali catalyst, methanol and vegetable oil are fully mixed to form reaction raw material liquid, the reaction raw material liquid continuously enters from a feed inlet of the reactor and firstly enters into a reaction chamber at the lowest part of the reactor, a stirring shaft is driven by a motor, then a stirring blade is driven by the stirring shaft to stir the reaction raw material liquid, and meanwhile, independent heating and temperature control are carried out in each reaction chamber of the reactor through a coil pipe heat exchanger, so that the reaction raw material liquid is fully heated and uniformly stirred in each reaction chamber, and the reaction raw material liquid is fully reacted; after a certain reaction chamber is filled with liquid, the liquid rises to the next reaction chamber through the liquid lifting holes on the partition plate, the rest is done in the same way, the materials continuously rise to the higher reaction chamber through the liquid lifting holes on the partition plate for reaction, and the product is finally discharged out of the reactor through the discharge hole.
The tower type continuous flow reactor is applied to the production of biodiesel through ester exchange reaction and is characterized in that the reaction temperature from the bottommost reaction chamber to the uppermost reaction chamber of the reactor is gradually reduced, the reaction temperature of the bottommost reaction chamber is 64-65 ℃, and the reaction temperature of the uppermost reaction chamber is 54-55 ℃.
The tower type continuous flow reactor is applied to the production of biodiesel through ester exchange reaction and is characterized in that the mass ratio of methanol to vegetable oil in a reaction raw material liquid is 1: 4.5-5.5, an alkali catalyst is KOH or NaOH, and the mass of the alkali catalyst is 0.8-1.2% of that of the vegetable oil; the total residence time of the reaction raw material liquid in the reactor is 30 to 60min, preferably 35 to 45 min.
The reactor of this application can be fine use in the production field of grease chemical industry, for example: the alkali catalyst, methanol and vegetable oil are fully mixed to form reaction raw material liquid, and the reaction raw material liquid is subjected to ester exchange reaction to produce the biodiesel, and the reaction is a reversible reaction. The transesterification reaction is divided into three steps, the first step is endothermic, and the initial high temperature is capable of increasing the reaction rate. And the second step and the third step of the ester exchange reaction are exothermic reactions, and the late cooling can promote the reaction balance to move to the right and increase the conversion rate. In the reactor, each reaction chamber is independently heated and controlled by the coil heat exchanger, so that the adaptive temperature control can be respectively carried out on each stage of the ester exchange reaction, and the conversion rate of the reaction can be effectively increased on the premise of effectively improving the reaction rate.
Compared with the existing reactor, the reactor of the application has the advantages that: (1) all the stirring paddles share one stirring shaft, the stirring speed of the whole tower is the same, and the regulation and control are more convenient; (2) the reactor is divided into multiple chambers by the plurality of partition plates, and the tower reactor occupies a small area, so that the volume utilization rate is improved, and the occupied area and the cost are reduced; furthermore, the number of layers and the number of the used layers can be designed according to actual conditions, and the reactor can be used as a single-layer reactor or a multilayer reactor, namely, one reactor can realize the functions of a plurality of reactors; (3) the reactor has stable operation condition, good mixing effect and controllable reaction condition of each layer, and can more conveniently regulate and control the operation of the reactor; (4) for the kettle-type reactor, the tower-type reactor can realize continuous production, shorten the reaction time, reduce back mixing, has higher efficiency and can bring higher economic and educational benefits.
Drawings
FIG. 1 is a schematic diagram of the structure of a column continuous flow reactor of the present application;
FIG. 2 is a schematic diagram of a baffle configuration for a column continuous flow reactor of the present application;
description of the drawings: 1-reactor, 2-discharge port, 3-heat exchanger, 4-stirring blade, 5-stirring shaft, 6-clapboard, 7-feed port, 8-liquid-lifting hole, 9-shaft hole, 10-motor, 11-sampling port, 12-liquid-discharging port, 13-pressure gauge, 14-thermodetector and 15-speed reducer.
Detailed Description
The present invention is further illustrated by the following examples, which should not be construed as limiting the scope of the invention.
Example (b): compare FIGS. 1-2
A tower type continuous flow reactor comprises a reactor 1 in a tower structure, wherein the top of the reactor 1 is provided with a motor 10, and the motor 10 is connected with a stirring shaft 5; the reactor is characterized in that a plurality of clapboards 6 are arranged in the reactor 1 from bottom to top at intervals, the clapboards 6 divide the reactor 1 into a plurality of reaction chambers, each clapboard 6 is provided with a plurality of liquid lifting holes 8 and a shaft hole 9 for penetrating the stirring shaft 5, and the shaft holes 9 on the plurality of clapboards 6 are positioned on the same vertical line. The lower end of the stirring shaft 5 extends into the reactor 1 from the top of the reactor 1 and extends to the bottom of the reactor 1 through the shaft hole 9 on the partition plate 6; in the reactor 1, at least one layer of stirring blades 4 is fixedly arranged on a stirring shaft 5 in each reaction chamber, and the ratio of the outer diameter of each stirring blade to the inner diameter of the reactor is 0.1-0.9: 1.
In reactor 1, the bottom of the reaction chamber of the below is equipped with feed inlet 7, and the upper portion of the reaction chamber of the top is equipped with discharge gate 2, and when letting in reaction liquid from feed inlet 7 to reactor 1, reaction liquid can pass through the liter liquid hole 8 on the baffle 6, reacts in passing through every reaction chamber of reactor 1 from the bottom up in proper order, and reaction product finally flows out from discharge gate 2. In comparison with FIG. 1, the bottom of the lowest reaction chamber is further provided with a tapping hole 12, and a tapping valve is arranged on the tapping hole 12. The bottom feed inlet 7 of the lowest reaction chamber is connected with a feed pump through a pipeline.
Referring to fig. 1, in a reactor 1, each reaction chamber is provided with a coil heat exchanger 3, and a coolant medium or a heat medium is respectively introduced into the coil heat exchanger 3 in each reaction chamber, so as to independently control the reaction temperature in each reaction chamber of the reactor 1; wherein, the inlet end and the outlet end of the coil heat exchanger 3 both penetrate out from the side wall of the reactor 1.
In the present application, a lift tube is fittingly installed on the lift hole 8 of each partition plate 6, and a check valve is installed on the lift tube, so that the reaction liquid in the reactor 1 can only flow from bottom to top. And the height of the liquid lifting pipe on the partition plate is 2-20 cm.
Furthermore, the aperture of the liquid lifting holes 8 on the partition plate 6 is 3-40 mm, and the number of the liquid lifting holes 8 on the partition plate 6 is 1-10; the total opening area of the liquid lifting holes on the partition plate is 5-50% of the area of the partition plate 6.
Furthermore, the number of reaction chambers formed by the reactor 1 being partitioned by the partition plates is 3-30.
Referring to fig. 1, in a reactor 1, each reaction chamber is provided with a temperature measuring instrument 14, the upper part of each reaction chamber is provided with a sampling port 11, and the uppermost reaction chamber is provided with a pressure gauge 13; the motor 10 is connected with the stirring shaft 5 through a speed reducer 15.
The first embodiment is as follows:
as shown in the figure 1-2, the tower type continuous flow reactor is of a tower type structure, 4 partition plates are arranged in the reactor, the 4 partition plates divide the reactor into five reaction chambers, each partition plate is provided with two liquid lifting holes and an axle hole, the diameter of each liquid lifting hole is 25mm, and the diameter of each axle hole is 140 mm. The reactor has a column internal diameter of 1m and a height of 0.5m per reaction chamber.
A coil heat exchanger is arranged in each reaction chamber, and the heat exchange area of the coil heat exchanger is 1m2The temperature in each reaction chamber is controlled by adjusting the flow of the heat exchange medium in the coil heat exchanger. Each reaction chamber is provided with a sampling port and a temperature measuring port, and the sampling port is provided with a valve.
The top of the reactor is provided with a motor, the motor is connected with a stirring shaft through a speed reducer, the lower end of the stirring shaft extends into the reactor from the top of the reactor and penetrates through a shaft hole in the partition plate to extend to the bottom of the reactor. In the reactor, a turbine stirring paddle is fixedly arranged on a stirring shaft in each reaction chamber, 5 turbine stirring paddles are arranged on the stirring shaft in total, and the outer diameter of each paddle is 0.5 m.
The working method of the reaction in this example is as follows: the raw material liquid continuously enters from the feeding hole, is pumped into the reactor by the feeding pump, firstly enters into the lowest reaction chamber of the reactor, is driven by the motor to stir by the stirring shaft, and then is driven by the turbine stirring paddle to stir the raw material liquid, and is controlled to the optimal temperature of the reaction by the coil pipe heat exchanger, so that the raw material liquid can be fully heated and uniformly stirred in each reaction chamber, and the raw material liquid can be fully reacted; when a certain reaction chamber is filled with liquid, the liquid rises to the next layer of reaction chamber through the liquid lifting holes on the partition plate, is continuously stirred by the turbine type stirring blades in the next layer of reaction chamber, is subjected to temperature control by the coil heat exchanger, and is continuously heated and reacts. And by analogy, the materials continuously rise into a higher reaction chamber through liquid lifting holes in the partition plate to react, and the product is finally discharged out of the reactor through a discharge hole.
Taking the transesterification of soybean oil and methanol as an example: the KOH catalyst dissolves in methanol to form a methanol-KOH solution. Mixing a methanol-KOH solution and soybean oil, wherein the mass of KOH is 1 percent of that of the soybean oil, the mass ratio of the methanol to the soybean oil is 1:5, heating the mixed solution of the methanol-KOH-soybean oil to 64.5 ℃, pumping the mixed solution into a first reaction chamber at the bottom of a reactor, gradually rising, and finally discharging the mixed solution from a last reaction chamber at the top of the reactor, wherein the temperature of each layer is independently controlled because the transesterification reaction of the methanol and the soybean oil is an exothermic reaction. From bottom to top, the temperature in the first reaction chamber was controlled at 64.5 deg.C, the temperatures in the second to fourth reaction chambers were controlled at 62.5 deg.C, 59.5 deg.C, and 54.5 deg.C, respectively, the stirring speed was 200rpm, and the residence time of the material in each chamber was 10 min. After the reaction product comes out from the top of the reactor, sampling and analyzing, the conversion rate of the soybean oil is 97.8%.
Claims (7)
1. A tower type continuous flow reactor is characterized in that the reactor (1) is of a tower type structure, the top of the reactor (1) is provided with a motor (10), and the motor (10) is connected with a stirring shaft (5); a plurality of clapboards (6) are arranged in the reactor (1) at intervals from bottom to top, the clapboards (6) divide the reactor (1) into a plurality of reaction chambers, each clapboard (6) is provided with a plurality of liquid lifting holes (8) and a shaft hole (9) for penetrating through the stirring shaft (5), and the shaft holes (9) on the clapboards (6) are positioned on the same vertical line;
the lower end of the stirring shaft (5) extends into the reactor (1) from the top of the reactor (1) and extends to the bottom of the reactor (1) through a shaft hole (9) in the partition plate (6); in the reactor (1), at least one layer of stirring blade is fixedly arranged on a stirring shaft (5) in each reaction chamber;
in reactor (1), the bottom of the reaction chamber of below is equipped with feed inlet (7), and the upper portion of the reaction chamber of the top is equipped with discharge gate (2), when letting in reaction liquid in reactor (1) from feed inlet (7), the reaction liquid can pass through rise liquid hole (8) on baffle (6), reacts in every reaction chamber through reactor (1) from the bottom up in proper order, and the reaction product finally flows from discharge gate (2).
2. A tower type continuous flow reactor according to claim 1, wherein in the reactor (1), each reaction chamber is provided with a coil heat exchanger (3), and a cooling medium or a heating medium is respectively introduced into the coil heat exchanger (3) in each reaction chamber so as to independently control the reaction temperature in each reaction chamber of the reactor (1); wherein, the inlet end and the outlet end of the coil heat exchanger (3) both penetrate out from the side wall of the reactor (1).
3. A continuous flow tower reactor according to claim 1 wherein the lift tubes are fitted to the lift holes (8) of each partition (6) and one-way valves are fitted to the lift tubes to allow the reaction liquid in the reactor (1) to flow only from the bottom up.
4. The tower type continuous flow reactor according to claim 1, wherein the diameter of the liquid lifting holes (8) on the partition plate (6) is 3-40 mm, and the number of the liquid lifting holes (8) on the partition plate (6) is 1-10; the total opening area of the liquid lifting holes on the partition plate is 5-50% of the area of the partition plate (6).
5. The continuous flow tower reactor of claim 3 wherein the height of the lift tube is 2-20 cm.
6. The continuous flow tower reactor of claim 1, wherein the ratio of the outer diameter of said stirring blades to the inner diameter of the reactor is 0.1 to 0.9: 1; the number of reaction chambers formed by the reactor (1) separated by the partition plate is 3-30.
7. A continuous flow tower reactor according to claim 1, wherein in the reactor (1) each reaction chamber is provided with a temperature measuring device (14), the upper part of each reaction chamber is provided with a sampling port (11), and the uppermost reaction chamber is provided with a pressure gauge (13); the motor (10) is connected with the stirring shaft (5) through a speed reducer (15).
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| CN202121622795.1U CN215389283U (en) | 2021-07-16 | 2021-07-16 | Tower type continuous flow reactor |
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| CN113398868A (en) * | 2021-07-16 | 2021-09-17 | 浙江工业大学 | Tower type continuous flow reactor and application thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113398868A (en) * | 2021-07-16 | 2021-09-17 | 浙江工业大学 | Tower type continuous flow reactor and application thereof |
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