CN110201624A - A kind of contiguous segmentation charging reactor for synthetic reaction - Google Patents

Abstract

The invention discloses a continuous segmented feed reactor for synthesis reaction, which comprises a three-layer jacket structure, the outermost layer is a heat exchange medium layer, and the heat exchange medium layer shell is provided with a heat exchange medium inlet and a heat exchange medium Outlet, a deflector is provided between the reactant shell and the jacket shell; the deflector is a spiral plate; the middle layer is the feed section of the reaction material A and the main reaction space, and the feed port of the reaction material A and the reaction Product outlet; the innermost central tube is the feed tube of the reaction material B; the outermost layer is the heat exchange medium channel, the heat exchange medium flows along the deflector plate and exchanges heat through the tube wall, and the heat exchange medium exits after the heat exchange is completed leave the reactor; the invention can realize the continuous addition of reaction materials, realize the continuous reaction, increase the output, reduce the operating cost, strengthen the heat transfer effect, and avoid the side reaction caused by the large local temperature difference. question.

Description

A continuous segmented feed reactor for synthesis reaction

technical field

The invention relates to the technical field of chemical reaction equipment, in particular to a continuous segmented feed reactor for synthesis reaction.

Background technique

At present, many chemical reactions are involved in the production process of pharmaceuticals and fine chemicals. Some chemical reactions involve multiple materials, and a large amount of reaction heat will be absorbed or released during the reaction process, and the selectivity and conversion rate of the reaction process are affected by temperature conditions. Therefore, the heat exchange and temperature control during the reaction are very important to improve the reaction selectivity and conversion rate.

Chemical synthesis reactions in the production process of pharmaceuticals and fine chemicals are usually carried out in tank reactors, and heat exchange is carried out by setting jackets on the synthesis tanks. However, due to the small heat transfer area, the mass transfer and heat transfer efficiency are low. To avoid Due to the untimely mass transfer and heat transfer, the side reaction affects the product yield, so only intermittent feeding can be adopted, which leads to too long feeding time and affects the output.

CN201420196752.5 discloses a three-layer glass reactor belonging to the technical field of chemical reaction equipment, including a frame, a reactor body, a constant pressure funnel, a condenser and a stirring device extending into the reactor body, and the constant pressure funnel and the condenser are respectively connected Reactor body, the reactor body is a three-layer glass reactor body, the frame is provided with a lifting positioning plate and a kettle tray, the reactor body is connected with the frame through the positioning plate, and the kettle tray is located on The lower part of the reactor body. This utility model adds a third layer of glass as a vacuum heat insulation layer on the basis of the original double-layer glass, which increases the heat insulation efficiency by 25%, reduces the area of the kettle body by 1㎡, and reduces energy consumption by 15%; high borosilicate glass (GG17) is used The main body of the reaction kettle is made, so that the temperature resistance of the reaction kettle can reach -120°C-+250°C. The device has high heat insulation efficiency, corrosion resistance and wear resistance. CN201320353141.2 discloses a reaction kettle for improving the strength of the heat-exchange jacket, comprising a kettle body with a heat-exchange jacket and an insulation jacket wrapped in the heat-exchange jacket, the heat-insulation jacket includes The thermal insulation material layer of the cover, the anti-loose net tightly attached to the thermal insulation material layer and the protective shell outside the anti-loose net. The thermal insulation cover has a three-layer structure, and the anti-loosening net in the middle layer can make the three layers of materials tightly connected, and at the same time, it can also significantly improve the strength of the thermal insulation cover, prevent the wear and tear of the thermal insulation cover, and prolong the service life of the thermal insulation cover. CN201410327700.1 discloses a swept-back high-efficiency hot plate diversion rectification multi-phase reactor, including a cylindrical kettle body, the kettle body is set upright, and the side wall of the kettle body is sequentially provided with a discharge port, a liquid inlet The feed port and the gas feed port are provided with a central shaft connected to an external motor in the longitudinal direction of the kettle body. Between the outer end of the kettle body and the inner wall of the kettle body, there are 6-10 high-efficiency heat exchange and diversion rectification devices. The inner wall of the kettle body is evenly distributed with 4-6 pieces of side wall diversion full baffles. There is a liquid jet distributor connected to the liquid feed port and a gas jet distributor connected to the gas feed port. There is an overflow area in the kettle body, and the reaction product is extracted from the discharge port through the overflow area. The advantage is that it can realize The multi-phase system has good mixing effect, large heat transfer area, and precise temperature control. The swept-back high-efficiency hot plate diversion rectification multi-phase reactor. However, in the prior art, it is the mode of intermittent feeding, the efficiency is general, and the output is not high.

Therefore, in order to enhance the mixing rate of materials and product yield, and increase product output, heat transfer needs to be enhanced. There is an urgent need for a continuous production system and a new Reactor, so as to realize the continuous production process and greatly improve the production capacity of the device.

Contents of the invention

In view of this, the present invention proposes a kind of continuous subsection feed reactor for synthetic reaction, to solve above technical problem;

In order to achieve the above object, the present invention adopts the following technical solutions to realize:

A continuous segmented feed reactor for synthesis reactions, including a three-layer jacket structure, the outermost layer is a heat exchange medium layer, and the heat exchange medium layer shell is provided with a heat exchange medium inlet and a heat exchange medium outlet, for Enhance the heat exchange effect. A deflector is set in the heat exchange medium layer to promote fluid turbulence; that is, a deflector is set between the reactant shell and the jacket shell;

Preferably, the deflector is a spiral plate;

Preferably, the middle layer is a reaction material A feed section and a main reaction space, and is provided with a reaction material A feed inlet and a reaction product outlet;

The innermost central tube is the feed tube for the reaction material B;

The outermost layer is the heat exchange medium channel. The heat exchange medium flows along the guide plate and exchanges heat through the tube wall. After the heat exchange is completed, the heat exchange medium exits the reactor;

Preferably, after the reaction material A is metered, it enters the intermediate reaction channel continuously from the reaction material A feed port; after the reaction material B is metered, it enters the innermost central tube from the reaction material B feed port, and on the innermost central tube There are reaction material B distribution holes in each section, which are connected with the intermediate reaction channel between the reactor shell and the innermost central tube, so that the reaction material B can be continuously added to the reaction material A through the reaction material B distribution holes in sections. to react;

Preferably, the flange distributor is placed on the innermost central pipe, and the reaction material B distribution pipe is fixedly penetrated into the hole on the flange distributor, and passes through the reactor shell through the reaction material B distribution hole below it;

At the same time, because the reaction material B is added vertically, it is easier to mix with the reaction material A evenly, which promotes the reaction and mass transfer and heat transfer; because the reaction material B is continuously added in sections, the reaction material is added after the heat transfer of the previous stage of reaction is completed. B. It is easier to control the temperature of the reactor, avoiding the disadvantages of increased side reactions caused by untimely heat exchange due to continuous feeding of materials from a single feed port; at the other end of the reactor, the reaction is completed, and the reaction product is discharged from the outlet.

Preferably, there are multiple distribution pipes for the reaction material B, with "L"-shaped elbows on both sides, and a middle pipe type elbow; the distribution hole of the reaction material B is horizontally placed on the innermost center pipe along the circumferential direction of the flange distributor; the length of the "L" type elbow increases successively along the vertical direction, and the The curved pipe has the longest length in the vertical direction and is placed at the bottom of the innermost central pipe;

Preferably, there are two inlets for the reaction material A, placed on both sides of the inlet for the reaction material B;

Preferably, the reaction material B distribution pipe is arranged axisymmetrically on the outer wall of the innermost central tube with respect to the direction of the central axis of the reaction material B feed port.

Preferably, the reaction material B distribution pipe and the reaction material distribution hole are detachably installed.

A continuous segmented feed reactor for synthesis reaction of the present invention is set in a three-layer jacket structure, the outermost layer is a heat exchange medium layer, and the heat exchange medium enters the reactor through the heat exchange medium inlet on the shell and The reaction materials are subjected to heat exchange between partition walls, and the heat exchange medium flows out of the reactor from the outlet after heat exchange. In order to enhance the heat exchange effect, a spiral plate is arranged in the heat exchange medium layer to promote fluid turbulence. The middle layer is the feed section of the reaction material A and the main reaction space. After being metered, the reaction material A continuously enters the middle reaction channel from the feed port of the reaction material A and reacts with the reactant B added from the innermost layer of the reactor. The reaction proceeds At the same time, it also exchanges heat with the outer heat exchange medium to maintain a constant reaction temperature; the innermost central tube is the feed tube for the reaction material B, and the reaction material B enters the innermost central tube from the feed port of the reaction material B after metering. , on the innermost central tube, the section openings are connected to the middle reaction channel, so that the reaction material B can be continuously added to the reaction material A in sections for reaction, or the material can be dispersed to multiple reaction materials B by using a flange distributor The distribution pipe is then added to the reaction material A in sections; at the same time, due to the vertical addition of the reaction material B, it is easier to mix evenly with the reaction material A, which promotes the reaction and mass transfer and heat transfer; because the reaction material B is continuously added in sections, It is easier to keep the temperature of the reactor constant by adding the reaction materials after the heat transfer of the previous stage of the reaction is completed, and avoid the disadvantages of increasing side reactions due to untimely heat exchange caused by continuous feeding of materials from a single feed port. At the other end of the reactor, The reaction is completed, and the reaction product is discharged from the outlet.

The technical solution of the present invention has at least the following advantages and beneficial effects:

1) The present invention can realize the continuous addition of reaction materials, realize the continuity of reaction, improve output, and reduce operating cost;

2) The present invention significantly increases the heat transfer coefficient, strengthens the heat transfer effect, and avoids the problem of side reactions caused by large local temperature differences;

3) The present invention can flexibly control the heat transfer distance and heat transfer area, which is beneficial to the control of reaction temperature;

4) The present invention has high volume utilization rate, high production capacity of a single set of equipment, significantly reduced floor space and investment.

Description of drawings

Fig. 1 is a cross-sectional structure diagram of a reactor in which the reactant material B provided by the present invention is fed in stages through distribution pipes.

Fig. 2 is a full cross-sectional structure diagram of a reactor in which the reaction material B adopts the distribution hole feeding type provided by the present invention.

Detailed ways

The present invention will be described below in conjunction with the accompanying drawings and specific embodiments.

In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below in conjunction with the accompanying drawings. Apparently, the described embodiments are some, not all, embodiments of the present invention.

Therefore, the following detailed description of the embodiments of the present invention is not intended to limit the scope of the claimed invention, but merely represents some embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by persons of ordinary skill in the art without creative efforts fall within the protection scope of the present invention.

It should be noted that like numerals and letters denote similar items in the following figures, therefore, once an item is defined in one figure, it does not require further definition and explanation in subsequent figures.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", The orientation or positional relationship indicated by the "rear side" is based on the orientation or positional relationship shown in the drawings, or the orientation or positional relationship that is usually placed when the product of the invention is used. Such terms are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention.

It should also be noted that, in the description of the present invention, unless otherwise clearly stipulated and limited, the terms "setting", "installation", "connection" and "connection" should be understood in a broad sense, for example, it may be a fixed connection, It can also be a detachable connection or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediary, and it can be the internal communication of two components. Those skilled in the art can understand the specific meanings of the above terms in the present invention according to specific situations.

As shown in Figure 1-2, the present invention provides a continuous staged feed reactor for synthesis reaction, which includes a three-layer jacket structure, the outermost layer is a heat exchange medium layer, and the outer shell of the heat exchange medium layer is provided with The heat exchange medium inlet 2 and the heat exchange medium outlet 1 are equipped with a deflector 7 in the heat exchange medium layer to enhance the heat exchange effect to promote fluid turbulence; that is, a deflector is provided between the reactant shell 8 and the jacket shell 9 7;

As a preferred embodiment of the present invention, the deflector 7 is a spiral plate;

As a preferred embodiment of the present invention, the middle layer is a reaction material A feed section and a main reaction space, and is provided with a reaction material A feed inlet 3 and a reaction product outlet 10;

The innermost central tube 11 is the feed tube for the reaction material B;

The outermost layer is the heat exchange medium channel, the heat exchange medium flows along the deflector 7 and exchanges heat through the tube wall, and leaves the reactor through the heat exchange medium outlet 1 after the heat exchange is completed;

As a preferred embodiment of the present invention, the reaction material A enters the middle reaction channel continuously through the reaction material A feed port 3 after being metered; the reaction material B enters the innermost central tube through the reaction material B feed port 4 after metering 11. There are reaction material B distribution holes 6 segmented on the innermost central tube 11, which communicate with the intermediate reaction channel between the reactor shell 8 and the innermost central tube 11, so that the reaction material B can be segmented Continuously pass through the distribution hole 6 of the reaction material B and add it into the reaction material A for reaction;

As a preferred embodiment of the present invention, the flange distributor 5 is placed on the innermost central pipe 11, and the reaction material B distribution pipe 12 is fixedly penetrated into the hole on the flange distributor 5, and the reaction material B passing through it below The distribution hole 6 passes through the reactor shell 8;

Further, the reaction material B distribution hole 6 is placed on the innermost central tube 11;

At the same time, because the reaction material B is added vertically, it is easier to mix with the reaction material A evenly, which promotes the reaction and mass transfer and heat transfer; because the reaction material B is continuously added in sections, the reaction material is added after the heat transfer of the previous stage of reaction is completed. B. It is easier to control the temperature of the reactor, avoiding the disadvantages of increased side reactions caused by untimely heat exchange due to continuous feeding of materials from a single feed port; at the other end of the reactor, the reaction is completed, and the reaction product is discharged from the outlet.

As a preferred embodiment of the present invention, there are multiple distribution pipes 12 for the reaction material B, with "L"-shaped elbows on both sides and a middle one type elbow; the reaction material B distribution hole 6 is horizontally placed on the innermost central tube 11 along the circumferential direction of the flange distributor 5; the length of the "L" type elbow increases successively along the vertical direction, and the The curved pipe is the longest along the vertical length and is placed at the bottom of the innermost central tube 11;

As a preferred embodiment of the present invention, there are two feed ports 3 for the reaction material A, placed on both sides of the feed port 4 for the reaction material B;

As a preferred embodiment of the present invention, the reaction material B distribution pipe 12 is arranged axisymmetrically on the outer wall of the innermost central tube 11 with respect to the direction of the central axis of the reaction material B feed port 4;

As a preferred embodiment of the present invention, the reaction material B distribution pipe 12 and the reaction material B distribution hole 6 are detachably installed.

As shown in Fig. 1-2, a kind of continuous subsection feeding reaction processing method that is used for synthetic reaction, concrete implementation steps are as follows:

1) Metering the reaction material A and the reaction material B;

2) The metered reaction material A is continuously entered into the intermediate reaction channel through the reaction material A feed port 3, and the metered reaction material B is entered into the innermost central tube 11 through the reaction material B feed port 4, and the reaction material B is continuously added to the reaction material A in sections through the distribution holes 6 of the reaction material B to react;

3) At the other end of the reactor, the reaction is completed, and the reaction product is discharged from the reaction product outlet 10 .

As a preferred embodiment of the present invention, the reaction material B uses the flange distributor 5 to disperse the material to a plurality of reaction material B distribution pipes 12 and then adds it to the reaction material A in stages.

The above embodiments are only used to illustrate but not limit the technical solution of the present invention. Any modification or partial replacement that does not depart from the spirit of the present invention shall fall within the scope of the claims of the present invention.

Claims (9)

1. a kind of contiguous segmentation for synthetic reaction feeds reactor, it is characterised in that: including three layers of jacket structured, outermost layer For heat transferring medium layer, it is provided with heat transferring medium import (2) and heat transferring medium outlet (1) on heat transferring medium layer shell, is changed for enhancing It is equipped with deflector (7) in thermal effect heat transferring medium layer and promotes Hydrodynamic turbulence；I.e. between reactant shell (8) and collet shell (9) Equipped with deflector (7)；

The deflector (7) is spiral plate；

Middle layer is reaction mass A feed zone and key reaction space, is equipped with reaction mass A feed inlet (3) and reaction product goes out Mouth (10)；

Innermost layer central tube (11) is reaction mass B feed pipe；

Outermost layer is heat exchanging medium passage, and heat transferring medium is flowed along deflector (7) and exchanged heat by tube wall, after the completion of heat exchange Reactor is left by heat transferring medium outlet (1).

2. a kind of contiguous segmentation for synthetic reaction according to claim 1 feeds reactor, it is characterised in that: reaction Material A is continuously entered in intermediate reaction channel by reaction mass A feed inlet (3) after metering；Reaction mass B is after metering by anti- Material B feed inlet (4) is answered to enter innermost layer central tube (11), segmentation is provided with reaction mass B points on innermost layer central tube (11) Cloth hole (6), the intermediate reaction channel between shell of reactor (8) and innermost layer central tube (11) are connected.

3. a kind of contiguous segmentation for synthetic reaction according to claim 2 feeds reactor, it is characterised in that:

Flange distributor (5) is placed on innermost layer central tube (11), and reaction mass B distributor pipe (12) is fixed to penetrate into flange distribution Hole on device (5) is pierced by shell of reactor (8) by reaction mass B distribution hole (6) below.

4. a kind of contiguous segmentation for synthetic reaction according to claim 3 feeds reactor, it is characterised in that:

The reaction mass B distributor pipe (12) be it is multiple, two sides be " L " type bend pipe, centre be " ⊥ " type bend pipe；The reactant Material B distribution hole (6) is horizontally placed on innermost layer central tube (11) along flange distributor (5) circumferencial direction；" L " type bend pipe edge Vertical direction length successively increases, and " ⊥ " type bend pipe length longest along the vertical direction is placed in innermost layer central tube (11) Bottom.

5. a kind of contiguous segmentation for synthetic reaction according to claim 2 feeds reactor, it is characterised in that:

The reaction mass A feed inlet (3) is two, is placed in the two sides of reaction mass B feed inlet (4).

6. a kind of contiguous segmentation for synthetic reaction according to claim 4 feeds reactor, it is characterised in that:

The reaction mass B distributor pipe (12) is on innermost layer central tube (11) outer wall about reaction mass B feed inlet (4) center Axis direction is arranged at axial symmetry.

7. a kind of contiguous segmentation for synthetic reaction according to claim 3 feeds reactor, it is characterised in that:

The reaction mass B distributor pipe (12) and reaction mass B distribution hole (6) are detachably installed.

8. a kind of contiguous segmentation for synthetic reaction feeds reaction treatment method, which is characterized in that specific implementation step is as follows:

1) reaction mass A and reaction mass B are measured；

2) reaction mass A after metering is continuously entered into intermediate reaction channel by reaction mass A feed inlet (3), it will be through measuring Reaction mass B afterwards enters innermost layer central tube (11) by reaction mass B feed inlet (4), and reaction mass B passes through reaction mass B Distribution hole (6) zonal cooling, which is added in reaction mass A, to be reacted；

3) in the reactor other end, reaction is completed, and reaction product is discharged from reacting product outlet (10).

9. a kind of contiguous segmentation for synthetic reaction according to claim 8 feeds reaction treatment method, feature exists In:

In step 2), the reaction mass B utilizes flange distributor (5) by material dispersion to reaction mass B distributor pipe (12) Then segmentation is added in reaction mass A.