CN217189544U

CN217189544U - Reactor for three-phase reaction continuous production

Info

Publication number: CN217189544U
Application number: CN202220169741.2U
Authority: CN
Inventors: 杨钧尹; 陆益烽; 杨栽根; 陆有军
Original assignee: Taizhou Liancheng Chemical Equipment Co Ltd
Current assignee: Taizhou Liancheng Chemical Equipment Co Ltd
Priority date: 2022-01-21
Filing date: 2022-01-21
Publication date: 2022-08-16
Anticipated expiration: 2032-01-21

Abstract

The utility model discloses a reactor for three-phase reaction continuous production, including gas-liquid separation barrel (A1), reaction barrel (A2), reaction barrel two (A3), gas phase distribution room (A4), quick-witted case (A5), micropore sintered plate (II, III and IV) and temperature sensor (T1, T2 and T3), pressure sensor (P1, P2 and P3) to and agitating unit (V, VI, VII, VIII and IX), adjacent part is with flange joint. The utility model discloses a pipeline reactor for three-phase reaction serialization production, through the effect of this kind of micropore sintering board dispersion and garrulous gas phase bubble and the radial shearing of agitating unit in the first order reactor and the design of axial propulsion, reached the intensive mixing of gas-liquid-solid three-phase multidimension degree to greatly improved mass transfer and heat transfer effect, and the purpose of serialization production; meanwhile, the reaction volume of the reactor is small, so that the safety coefficient of the hydrogenation reaction is greatly improved.

Description

Reactor for three-phase reaction continuous production

Technical Field

The utility model belongs to the technical field of chemical industry equipment, concretely relates to a reactor for three-phase reaction continuous production.

Background

In the chemical production processes of medicines, pesticides, dyes, new materials, electronic chemicals and the like, three-phase reactions such as gas, solid, liquid and the like are often required to perform conversion of certain functional groups, such as the most classical hydrogenation catalytic reaction and the like. It is well known that the key factors affecting three-phase reaction rates, chemoselectivity and conversion are mass and heat transfer issues such as whether the reactants are in intimate contact instantaneously, whether the reaction temperature at each site can be tightly controlled, and the size of the gas bubbles.

The traditional kettle type reactor has the defects of mass transfer, heat transfer and the like, so that the reaction rate is low, the reaction selectivity is poor, the product yield is low, and the purification is difficult. And the liquid holdup in the production process is large, so that the safety production risk is invisibly increased.

The microchannel reactor proposed in recent years really brings great changes to the chemical industry, but the production process with solid participating in the reaction cannot be realized because the channel of the reactor is too small.

CN209138373U, CN108465454, CN108514855, etc. disclose a mixed reactor, which has enjoyable success in replacing some traditional kettle type reactions in liquid-liquid, gas-liquid, etc. two-phase reactions. However, the application of the method in a reaction system with both solid and gas also has the problems of poor mass transfer effect, overlarge pressure drop, too short residence time of reactants and the like.

The reactor disclosed in CN212215458U, although solving the continuous production problem of partial three-phase reaction, still has the problems of affecting the reaction rate, such as partial deposition of solid phase with high density, and easy aggregation and enlargement of bubbles with gas phase.

SUMMERY OF THE UTILITY MODEL

The utility model provides a reactor for three-phase reaction continuous production, which adopts the design of two-stage series reaction cylinder bodies comprising a micropore sintering plate, a forced stirring device, a fixed bed and the like which are beneficial to the micro-crushing distribution of gas-phase bubbles, thereby not only ensuring the gas-liquid-solid three-phase mixing effect, but also greatly reducing the pressure drop of a pipeline; and because the two-stage series reaction can be realized, the production requirements can be met in a customized manner according to the reaction activities of various substrates.

A reactor for three-phase reaction continuous production comprises a gas-liquid separation cylinder body (A1), a first reaction cylinder body (A2) and a second reaction cylinder body (A3), a gas phase distribution chamber (A4), microporous sintering plates (II, III and IV), stirring devices (V, VI, VII, VIII and IX), temperature sensors (T1, T2 and T3), pressure sensors (P1 and P2) and a liquid level sensor (L1), and is characterized in that the outer side of the reaction cylinder body is provided with a heating/cooling jacket; the gas-liquid separation cylinder is arranged at the uppermost part of the reaction cylinder, and a defoaming net (I) is arranged near the upper outlet of the gas-liquid separation cylinder; the micropore sintering plate is arranged between the two flanges at the joint of each cylinder body; the stirring device is arranged in the second lower reaction barrel (A3) and is used for magnetic stirring; the temperature sensor and the pressure sensor are arranged at proper positions of the cylinders; the cylinders are connected in series by flanges and/or welding.

Preferably, the cylinders are connected from top to bottom in sequence as a gas-liquid separation cylinder (A1), a reaction cylinder I (A2), a reaction cylinder II (A3) and a gas-phase distribution chamber (A4). Preferably, the cylinders are connected by flanges and/or welding, and more preferably by flanges.

Preferably, microporous sintered plates with different apertures are arranged in the middle of the flange at the joint of each cylinder body and are used for re-dispersing and filtering gas phase; more preferably, the pore diameters of the microporous sintered plates from top to bottom are respectively 0.22-0.45 um (microporous sintered plate II), 0.45-2.0 um (microporous sintered plate III) and 0.45-5.0 um (microporous sintered plate IV).

Preferably, at least 2 reactant inlets, 1 hydrogen inlet, 2 jacket cold/heat medium inlets and outlets, 2 temperature sensor mounting holes and 1 pressure sensor mounting hole are arranged in the second reaction cylinder (A3); preferably, the connecting flanges at the two ends of the second reaction cylinder (A3) adopt a thin and dense-hole sieve plate or a fence plate with high mechanical strength, and further preferably a fence plate.

Preferably, the outer layer of the second reaction cylinder (A3) is provided with a second interlayer (B2), and a diversion spiral plate (X) is arranged in the interlayer. The width of the interlayer is 10-100 mm, and the preferable width is 20-50 mm. Preferably, the interlayer is divided into 1-5 compartments, each compartment is provided with an inlet and an outlet, and more preferably, the inlets are connected in parallel.

Preferably, the first reaction cylinder (A2) is provided with a liquid outlet, 1 temperature sensor mounting hole and/or 1 pressure sensor mounting hole; preferably, the connecting flanges at the two ends of the first reaction cylinder (A2) adopt a thin and dense-hole sieve plate or a fence plate with high mechanical strength, and further preferably a fence plate.

Preferably, the outer side of the first reaction cylinder body (A2) is provided with an interlayer (B1), and a diversion spiral plate (X) is arranged in the interlayer. The width of the interlayer is 10-100 mm, and more preferably 20-50 mm. Preferably, the interlayer is divided into 1-3 compartments, each compartment is provided with an inlet and an outlet, and more preferably, the inlets are connected in parallel.

Preferably, the gas-liquid separation cylinder (a1) is provided with 1 liquid outlet, 1 gas outlet, 1 defoaming net, 1 liquid level sensor, 1 pressure sensor mounting hole and 1 liquid level sensor mounting hole. Preferably, the gas outlet is arranged at the upper top end of the gas-liquid separation cylinder, the liquid outlet is arranged on the cylinder close to the flange, the liquid level sensor is arranged at the lower third of the height of the gas-liquid separation cylinder, the defoaming net is arranged at the half of the height of the gas-liquid separation cylinder, and the pressure sensor is arranged at the upper third of the height of the gas-liquid separation cylinder.

Preferably, the gas phase distribution chamber (a4) is provided with a hydrogen inlet, a stirring shaft support and a permanent magnet. The stirring shaft is supported and fixed on the totally closed flange plate of lower extreme, the totally closed flange plate of lower extreme with gas phase distribution room (A4) seal weld, the upper end flange of gas phase distribution room (A4) is for adopting high mechanical strength's slim, dense hole sieve or fence board, further preferred fence board. The permanent magnet is fixed at one end of the stirring shaft, and the permanent magnet penetrates through the sintering plate and is sealed and fixed by a tetrafluoro shaft sleeve.

Preferably, the volume ratio of the second reaction cylinder (A3), the first reaction cylinder (A2), the gas-liquid separation cylinder (A1) and the gas-phase distribution chamber (A4) is 20-200: 10-80: 2-30: 1, and more preferably 20-50: 5-10: 1-5: 1.

Preferably, the stirring motor is a variable frequency motor, a rotating shaft of the variable frequency motor is connected with another permanent magnet and sealed in a case (A5), and the case (A5) is connected with a totally-enclosed flange plate at the lower end of the gas phase distribution chamber (A4) by a flange. Preferably, the rotating speed of the variable frequency motor is 0-1200 r/min, and further preferably 150-350 r/min.

Preferably, one end of the lower end of the stirring shaft after penetrating through the center of the micropore sintering plate (IV) is provided with a permanent magnet, and the middle of the stirring shaft between the permanent magnet and the micropore sintering plate is fixed on a support in the gas phase distribution chamber (A4) by adopting a bearing; the other end is fixed on a shaft support on an upper end flange of a second reaction cylinder body (A3).

Preferably, the paddle is welded on the stirring shaft by adopting 2 support legs, and the ratio of the radial expansion length of the paddle to the inner diameter of the reaction cylinder is 0.6-0.9: 1, and further preferably 0.7-0.9: 1. Preferably, the included angle between the blade surface of the paddle and the stirring shaft is 0-90 degrees, and further preferably 3-15 degrees. Preferably, the blade surface is regularly respectively a plurality of diameter be 2 ~ 10mm round hole, and the diameter of round hole is further preferred 3 ~ 5 mm.

Preferably, the blades are symmetrically arranged at two sides of the stirring shaft at 180 degrees, and two blades form a group; the distance between adjacent edges of the two adjacent groups of blades is 0-50 mm, and the preferable distance is 10-40 mm; and the included angle between two adjacent groups of blades is 90 degrees.

In a preferred embodiment of the present invention, the reaction cylinder may be set to 2 modes, one mode (a) is a combination of the reaction cylinder two (A3) and the reaction cylinder one (a2) in series, and the other mode (B) is only the reaction cylinder two (A3).

It should be noted that, the "inlet" or "outlet" in the above technical solutions is mainly compared with the general flow direction of the material, where the "inlet" corresponds to the material inlet, and the "outlet" corresponds to the material outlet.

Drawings

FIG. 1 is a schematic structural diagram of a three-phase reaction continuous production reactor of the present invention.

Detailed Description

The present invention will be further described with reference to fig. 1. It is to be understood that the drawings illustrate only preferred embodiments of the invention and are not to be considered limiting of its scope.

A reactor for three-phase reaction continuous production comprises a gas-liquid separation cylinder body (A1), a reaction cylinder body I (A2), a reaction cylinder body II (A3), a gas-phase distribution chamber (A4), a case (A5), microporous sintering plates (II, III and IV), temperature sensors (T1-T3), pressure sensors (P1 and P2) and stirring devices (V, VI, VII, VIII and IX), wherein adjacent parts are connected by flanges, the reactor is characterized in that a defoaming net (I) is arranged in the gas-liquid separation cylinder body (A1), a gas outlet (a) and the pressure sensors (P1) are arranged at the top end, a discharge outlet (b) and a liquid level sensor (L1) are arranged at the position close to the bottom, and a sieve plate type or grid type flange is arranged at the lower end; the inner cavity of the first reaction cylinder (A2) can be filled with solid-phase reactants and is provided with a temperature sensor (T1) and a pressure sensor (P2), a liquid/dirt discharge opening (e) is arranged near the bottom, a first jacket (B1) for heating or cooling is arranged on the outer side, and both ends of the first jacket are provided with sieve plate type or fence type flanges; a stirring device (V, VI, VII, VIII and IX), a temperature sensor (T2, T3) and a pressure sensor (P3) are arranged in the second reaction cylinder body (A3), screen plate type or fence type flanges are arranged at two ends, a stirring shaft fixing piece (VII) is arranged at the center of the flange at one end, at least 2 feed inlets (g and h) are arranged on the wall of the other end, and a second jacket (B2) for heating or cooling is arranged at the outer side of the second reaction cylinder body; one end of the gas phase distribution chamber (A4) is provided with a sieve plate type or fence type flange, the other end is provided with a sealing plate type flange, the center part of the inner side of the plate type flange is provided with a stirring shaft fixing frame (VII), a permanent magnet (V) connected with the stirring shaft is arranged in the fixing frame, and a cylinder body of the fixing frame is provided with a hydrogen inlet (k); a permanent magnet (V) connected with a rotating shaft of the motor is arranged in the case (A5), a flange is arranged at one end, and the other end is closed and provided with the motor (VI).

The stirring device comprises a motor VI, 2 permanent magnets (V), a stirring shaft (VIII), a blade (IX), 2 stirring shaft supports (VII) and a tetrafluoro shaft sleeve; the stirring shaft (VIII) and the blades (IX) are arranged in a second reaction cylinder body (A3), and the 2 permanent magnets (V) are respectively arranged in the gas phase distribution chamber (A4) and the case (A5); the 2 stirring shaft supports (VII) are respectively arranged on the inner side of a totally-enclosed plate type flange of the gas phase distribution chamber (A4) and the inner side of an upper end flange of the reaction cylinder II (A3); the 3 microporous sintering plates are respectively arranged between the connecting flanges of the gas-liquid separation cylinder body (A1) and the reaction cylinder body I (A2), between the connecting flanges of the reaction cylinder body I (A2) and the reaction cylinder body II (A3) and between the connecting flanges of the reaction cylinder body II (A3) and the gas-phase distribution chamber (A4). Particularly, a hole with the diameter of 2-5 times of that of the stirring shaft is formed in the center of a connecting flange of the second reaction cylinder (A3) and the gas phase distribution chamber (A4) and the micropore sintering plate, and the hole is used for the penetration of the stirring shaft and the installation of a PTFE sealing piece.

The outer side of the reaction cylinder I (A2) and the outer side of the reaction cylinder II (A3) are jacketed, and spiral guide plates are arranged in the reaction cylinder I and the reaction cylinder II; the heat exchanger can be respectively integrated, or can be respectively divided into a plurality of sections, and the same cooling medium or different cooling media are connected in parallel between the inlets and the outlets of the sections according to the process requirements.

The length-diameter ratio and the effective volume of each part of the reactor can be determined according to the calculation of specific reaction parameters of a production process, and the diameter of a reaction cylinder body is generally required to be not more than 500mm, and the length of the reaction cylinder body is not more than 6000 mm. Whether or not the reactor barrel (A2) is necessary for the reactor as a whole is determined by the residence time and the productivity required for a particular reaction.

As an implementation mode, during actual installation, the second reaction cylinder (A3) is fixed in place, then the stirring device penetrates into the second reaction cylinder (A3), the microporous sintering plate (IV) is sequentially installed, the tetrafluoro sealing element is installed, the permanent magnet connected with the inside of the gas phase distribution chamber (A4) is connected, and then the first reaction cylinder (A2) and the gas-liquid separation cylinder (A1) are sequentially installed. And finally, connecting and installing the LED chip with an external device according to process requirements.

It should be noted that, in the above technical solution, the "inlet" or the "outlet" is mainly compared with a general flow direction of the material, where the "inlet" corresponds to an inlet of the material, and the "outlet" corresponds to an outlet of the material.

Claims

1. A reactor for three-phase reaction continuous production comprises a gas-liquid separation cylinder body (A1), a reaction cylinder body I (A2) and a reaction cylinder body II (A3), a gas phase distribution chamber (A4), microporous sintering plates (II, III and IV), stirring devices (V, VI, VII, VIII and IX), temperature sensors (T1, T2 and T3), pressure sensors (P1, P2 and P3) and a liquid level sensor (L1); the device is characterized in that heating and/or cooling jackets are arranged on the outer sides of the first reaction cylinder body and the second reaction cylinder body; the gas-liquid separation cylinder is arranged at the uppermost part of the reaction cylinder, and a defoaming net (I) is arranged near the upper outlet of the gas-liquid separation cylinder; the micropore sintering plate is arranged at the joint of the cylinders and the lower end of the second reaction cylinder (A3) at the lowest part; the stirring device is arranged in the second reaction barrel body (A3) at the lowest part and is used for magnetic stirring; the temperature sensor and the pressure sensor are arranged at proper positions of the cylinders; the cylinders are connected in series by flanges and/or welding.

2. The reactor for three-phase reaction continuous production according to claim 1, wherein the second reaction cylinder (a3) comprises 2 reactant inlets (g and h), 1 hydrogen inlet (k), 2 jacket cold/heat medium inlets/outlets (j and f) and 2 temperature sensor mounting holes (T2 and T3), 1 pressure sensor mounting hole two (P2); the upper end of the reaction cylinder body I is connected with a reaction cylinder body I (A2) by a flange, a micropore sintering plate (III) is arranged between two flanges, the lower end of the reaction cylinder body I is connected with a gas phase distribution chamber (A4) by a flange, and a micropore sintering plate (IV) is arranged between two flanges; and an interlayer (B2) is arranged on the outer side of the second reaction cylinder body (A3), and a diversion spiral plate (X) is arranged in the interlayer.

3. A reactor for three-phase reaction continuous production according to claim 1, wherein the reaction cylinder one (a2) comprises 1 sewage drain (e) and one temperature sensor mounting hole (T1); the lower end of the reaction cylinder is connected with a second reaction cylinder (A3), the upper end of the reaction cylinder is connected with a gas-liquid separation cylinder (A1) by flanges, and a micropore sintering plate (II) is arranged between the two flanges; the outer side of the first reaction barrel body (A2) is provided with a first interlayer (B1), and a diversion spiral plate (X) is arranged in the interlayer.

4. A reactor for three-phase reaction continuous production according to claim 1, wherein the gas-liquid separation cylinder (a1) comprises a gas phase outlet (a), a reaction liquid outlet (b), a pressure sensor mounting hole one (P1), a liquid level sensor (L1) and a defoaming net (i); the lower end of the reaction cylinder is connected with a first reaction cylinder (A2) by a flange; the gas phase outlet (a) is arranged at the upper top end, and the reaction liquid outlet (b) is arranged near the connecting flange.

5. The reactor for three-phase reaction continuous production as claimed in claim 1, wherein the gas phase distribution chamber (A4) is arranged between the reaction cylinder II (A3) and the variable frequency motor set (VI), and comprises a hydrogen inlet (k) and a stirring shaft support member (VII), the upper end of the gas phase distribution chamber is connected with the reaction cylinder II (A3) by a flange, and the lower end of the gas phase distribution chamber is connected with the variable frequency motor set (VI) by a fully-closed flange; the stirring shaft support piece (VII) is arranged on a fully-closed flange, and the hydrogen inlet (k) is arranged on the gas phase distribution chamber (A4).

6. The reactor as claimed in claim 1, wherein the stirring device comprises a variable frequency motor set (VI), 2 permanent magnet modules (V), 2 supporting members (VII), a stirring shaft (VIII) and a plurality of blades (IX), the blades are installed on the stirring shaft and are arranged in the inner cavity of the second reaction cylinder (A3), two ends of the stirring shaft are respectively fixed on the upper end flange of the second reaction cylinder (A3) and the lower end flange plate of the gas phase distribution chamber (A4) by the supporting members (VII), the stirring shaft penetrates through the microporous sintering plate (IV), and the intersection is sealed by a tetrafluoro member.

7. The reactor for three-phase reaction continuous production according to claim 2 or claim 3, wherein the pressure resistance of the first reaction cylinder (A2) and the second reaction cylinder (A3) is 0.5-8 MPa, the effective volume of the reactor is determined according to specific production process conditions, and the length-diameter ratio of the second reaction cylinder (A3) is 1-100: 1.

8. A reactor for three-phase reaction continuous production according to claim 6, characterized in that the blades (IX) are provided with a plurality of circular holes and suitable inclination angles, having radial shearing and axial propelling functions, and the blades fill the cavity of the reaction cylinder body two (A3).

9. The reactor of claim 1, wherein the second reaction cylinder (A3) is used for continuous reaction of the powdery wear-resistant solid reactant and the gas-phase and liquid-phase reactants, and the first reaction cylinder (A2) is used for further continuous reaction of the granular solid reactant and the gas-phase and liquid-phase reactants.