CN217164344U - High conversion rate continuous flow reaction system - Google Patents

Abstract

The utility model belongs to the field of chemical equipment, and discloses a high-conversion-rate continuous flow reaction system, which comprises a micro-channel rapid reactor and a buffer reactor, wherein the micro-channel rapid reactor is internally provided with a micro-distributor and a reaction pipeline, the micro-distributor is internally provided with a material inlet and a flat cavity communicated with the material inlet, the flat cavity is communicated with the reaction pipeline, and the micro-channel rapid reactor is provided with a cold and heat medium inlet and a cold and heat medium outlet; a plurality of sections of heat exchange mixing units are arranged in the buffer reactor, and a cooling and heating medium inlet and outlet communicated with the heat exchange mixing units are arranged on the buffer reactor; one end of the reaction pipeline, which is far away from the micro-distributor, is communicated with the shell of the buffer reactor. The utility model discloses utilize microchannel fast reactor to realize thermal quick transfer, effectively reduce the side reaction to utilize the buffer reactor to further carry out the material reaction, thereby further improved the conversion rate, improved the yield of product.

Description

High-conversion-rate continuous flow reaction system

Technical Field

The utility model belongs to the chemical industry equipment field especially relates to a high conversion continuous flow reaction system.

Background

The chemical reactor is a device for realizing the reaction process and is widely applied to the fields of chemical industry, oil refining, metallurgy, light industry and the like. The chemical reactor is the core equipment of chemical production, and the advanced degree of the technology has important influence on the chemical production and directly influences the investment scale and the production cost of the device.

At present, the reaction synthesis process usually adopts a kettle type batch reaction, and the mass transfer and heat transfer efficiency of reaction materials is in a relatively low level, so that the reaction is not beneficial to the implementation of chemical reaction. Especially chemical reactions such as nitration, ammoniation and the like with high reaction rate and large heat release, the traditional kettle type and tubular reactors are difficult to transfer heat generated in the reaction process in time, and side reactions are increased, so that the yield of products is influenced, and the production cost is increased.

SUMMERY OF THE UTILITY MODEL

In view of the above-mentioned shortcomings of the prior art, the present invention is directed to a high conversion rate continuous flow reaction system, which is used to solve the problem that the product yield is affected by the heat generated in the reaction process which is difficult to timely transfer in the conventional kettle type and tubular reactor.

In order to achieve the above and other related objects, the present invention provides a high conversion rate continuous flow reaction system, which comprises a microchannel rapid reactor and a buffer reactor, wherein the microchannel rapid reactor comprises a microchannel rapid reactor shell, the microchannel rapid reactor shell is provided with a plurality of first feed inlets, the microchannel rapid reactor shell is internally provided with a micro distributor and a reaction pipeline, the micro distributor is internally provided with a plurality of material inlets and a plurality of flat cavities communicated with the corresponding material inlets, the material inlets are communicated with the corresponding first feed inlets, one ends of the flat cavities far away from the material inlets are communicated with the reaction pipeline, and the microchannel rapid reactor shell is provided with a cold and hot medium inlet and a cold and hot medium outlet; the buffer reactor comprises a buffer reactor shell, a plurality of sections of heat exchange mixing units are arranged in the buffer reactor shell, each section of heat exchange mixing unit comprises a heat exchange mixing element, each heat exchange mixing element consists of a plurality of staggered and coiled heat exchange tubes or a plurality of heat exchange tubes arranged in a matrix, and a plurality of cold and heat medium inlets and outlets communicated with the heat exchange tubes are arranged on the buffer reactor shell; and a second feeding hole and a second discharging hole are formed in the shell of the buffer reactor, and one end, far away from the micro distributor, of the reaction pipeline is communicated with the second feeding hole in the shell of the buffer reactor.

As mentioned above, the present invention provides a high conversion rate continuous flow reaction system, which has the following advantages:

1. the reaction materials enter the material inlet of the micro-distributor from the corresponding first feeding hole respectively, and form a film or a lamellar reaction material with small thickness in the flat cavity in the micro-distributor, namely, the reaction materials are converted into film or lamellar materials from strand-shaped (columnar) materials under the action of the micro-distributor, so that the contact area of two or more than two reaction materials (the types of the reaction materials can be set according to an actual production requirement book, and the number of the first feeding hole, the first material inlet and the flat cavity is correspondingly set) in a reaction pipeline is increased, the rapid mixing and mass transfer of the reaction materials are facilitated, and the reaction is facilitated. In the reaction process of the reaction materials in the reaction pipeline, the reaction rate is high, the heat release is large, the released heat is transmitted to the outer wall of the reaction pipeline through the inner wall of the reaction pipeline, and then is rapidly absorbed and taken out by a refrigerant in the shell of the micro-channel rapid reactor, so that the rapid transfer of the heat is realized, the occurrence of side reactions is effectively reduced, the conversion rate is improved, and the product yield is further improved.

2. Utilize microchannel fast reactor to shift the heat that the reaction process produced rapidly after, remaining reaction material is because reaction material and result change along with concentration, and its reaction rate slows down gradually, and the complete conversion still needs longer reaction time, continues to react in microchannel fast reactor and will influence the efficiency of entire system industrialization serialization production, consequently, the utility model discloses in, the reaction material behind microchannel fast reactor gets into and carries out further reaction in the buffer reactor to further improve the conversion rate and ensure entire system's handling capacity. And, the utility model provides a buffer reactor can make reaction material constantly mix, high-efficient heat transfer and distribute the dispersion in buffer reactor casing to improve mass transfer efficiency and heat transfer efficiency effectively.

Optionally, a plurality of baffles for obstructing the flow of the cooling and heating medium are arranged in the shell of the micro-channel rapid reactor.

In this scheme, utilize the baffling board to make the outer refrigerant of reaction tube have stronger turbulent strength to increase the heat transfer ability of system.

Optionally, the inner wall of the reaction pipe is provided with a plurality of baffling internals for obstructing the material flow.

In the scheme, the reaction materials are subjected to shear flow through the baffling internal parts in the reaction pipeline, so that the mass transfer of the reaction materials is enhanced.

Optionally, the number of microdistributor is more than two, the number of reaction pipeline is the same with the microdistributor, and reaction pipeline and microdistributor one-to-one, and the one end that the microdistributor was kept away from to the reaction pipeline is through second intercommunication of feed inlet on collecting pipe and the buffer reactor casing.

In the scheme, the number of the micro distributors is more than two, so that the treatment capacity of the micro-channel rapid reactor on reaction raw materials is improved. In addition, in the scheme, the micro-channel rapid reactor and the buffer reactor are communicated through the collecting pipe, and a plurality of communication sites are prevented from being arranged on the buffer reactor.

Optionally, the heat exchange mixing unit further comprises a filler, which is loaded in the gap between the buffer reactor shell and the heat exchange mixing element.

In the scheme, the filler can efficiently increase the mixing and flowing of reaction materials, and simultaneously increase the contact interface of gas-liquid two phases or liquid-liquid two phases, thereby realizing gas-liquid two phases, incompatible two phases and homogeneous reaction.

Optionally, the heat exchange mixing unit further comprises a filler support plate for supporting the filler and a filler press plate for compressing the filler, and both the filler support plate and the filler press plate are of sieve holes or sieve mesh structures.

In this scheme, utilize the backup pad that packs to support and pack and heat transfer mixing element, utilize the clamp plate that packs to compress tightly fixed packing, avoid packing to run off.

Optionally, a first distributor and a second distributor are arranged in the shell of the buffer reactor, two ends of the first distributor are respectively connected with the second feeding port and the heat exchange mixing unit close to the second feeding opening, and two ends of the second distributor are respectively connected with the second discharging port and the heat exchange mixing unit close to the second discharging port.

In this scheme, utilize first distributor and second distributor to get into the reaction material of buffering reactor and shunt.

Optionally, a temperature detection element is further arranged in the buffer reactor shell.

In this scheme, utilize the temperature detecting element to detect the temperature in the buffer reactor casing to the realization is to buffer reactor casing internal reaction temperature's control.

Optionally, the adjacent heat exchange tubes are arranged in an interweaving way at an angle of 60-120 degrees.

In the scheme, the heat exchange tubes are limited to be formed by interweaving 60-120 degrees between adjacent heat exchange tubes, so that the heat exchange mixing elements are distributed more reasonably.

Optionally, the reaction pipeline includes a plurality of reaction tubes, and two adjacent reaction tubes are communicated through a U-shaped tube.

In this scheme, two adjacent reaction shell and tubes pass through U type pipe intercommunication, can reduce the length of microchannel rapid reactor under the prerequisite that keeps the process of reaction material in microchannel rapid reactor the same.

Drawings

FIG. 1 is a schematic diagram of a high conversion rate continuous flow reaction system according to an embodiment of the present invention;

FIG. 2 is a longitudinal sectional view of a microchannel rapid reactor according to an embodiment of the present invention;

FIG. 3 is an axial cross-sectional view of a micro-distributor according to an embodiment of the present invention;

FIG. 4 is a cross-sectional view taken along line A-A of FIG. 3;

FIG. 5 is a longitudinal sectional view of a buffer reactor according to an embodiment of the present invention;

fig. 6 is a schematic structural diagram of a heat exchange mixing element in a buffer reactor according to an embodiment of the present invention.

Detailed Description

Reference numerals in the drawings of the specification include: the device comprises a raw material tank 1, a micro-channel rapid reactor 2, a buffer reactor 3, a product tank 4, a micro-channel rapid reactor shell 5, an inlet end tube plate 6, an outlet end tube plate 7, a first feed inlet 8, a micro distributor 9, a material inlet 901, a flat cavity 902, a reaction tube array 10, a collecting tube 11, a baffle plate 12, a cooling and heating medium inlet 13, a cooling and heating medium outlet 14, a buffer reactor shell 15, a first distributor 16, a second distributor 17, a heat exchange mixing element 18, a filler 19, a filler support plate 20, a filler press plate 21, a second feed inlet 22, a discharge outlet 23, a temperature detection element 24 and a cooling and heating medium inlet and outlet 25.

The following description is provided for illustrative purposes, and other advantages and features of the present invention will become apparent to those skilled in the art from the following detailed description.

Example one

As shown in fig. 1 to 6, the present example provides a high conversion rate continuous flow reaction system including a raw material tank 1, a microchannel rapid reactor 2, a buffer reactor 3, and a product tank 4. In this embodiment, the quantity of head tank 1 is two, splendid attire reaction material in two head tanks 1.

Referring to fig. 2, the microchannel fast reactor 2 includes a microchannel fast reactor shell 5, a left end of the microchannel fast reactor shell 5 is fixedly connected with an inlet end tube plate 6 (the fixed connection may be welding or may be through screw/bolt connection), a right end of the microchannel fast reactor shell 5 is fixedly connected with an outlet end tube plate 7, and a sealed space (for flowing of cooling and heating media) is formed between the inlet end tube plate 6, the microchannel fast reactor shell 5 and the outlet end tube plate 7. The left end of microchannel rapid reactor casing 5 is equipped with a plurality of feed inlets 8, be equipped with microdistrictor 9 and reaction tube in the microchannel rapid reactor casing 5, combine shown in fig. 3 and fig. 4, microdistrictor 9's inside is equipped with a plurality of material entry 901 and a plurality of flat chamber 902 that feed inlet 901 communicates with corresponding, in this embodiment, the quantity of material entry 901 and flat chamber 902 is two, the quantity of feed inlet 8 is two, two feed inlets 8 communicate with the material entry 901 that corresponds respectively, head tank 1 communicates with the feed inlet 8 that corresponds through the pipeline. The reaction pipeline comprises a plurality of reaction tubes 10, in this embodiment, the number of the reaction tubes 10 is three, the left end of the reaction tube 10 located at the bottom layer is communicated with the right end of the flat cavity 902, two adjacent reaction tubes 10 are communicated through a U-shaped tube, and the right end of the reaction tube 10 located at the top layer is communicated with a collecting tube 11. The inlet end tube sheet 6 and the outlet end tube sheet 7 can provide support for tubes such as reaction tubes 10.

The inner wall of each reaction tube row 10 is provided with a plurality of baffle internal parts (not shown) for blocking the flow of materials, in the embodiment, the baffle internal parts are welded on the inner wall of the reaction tube row; a plurality of baffle plates 12 for blocking the flow of the cooling and heating media are arranged in the microchannel rapid reactor shell 5, in this embodiment, the baffle plates 12 are welded on the inner wall of the microchannel rapid reactor shell 5, and the microchannel rapid reactor shell 5 is provided with a cooling and heating media inlet 13 and a cooling and heating media outlet 14.

As shown in fig. 5, the buffer reactor 3 includes a buffer reactor shell 15, a first distributor 16, a plurality of sections of heat exchange mixing units, and a second distributor 17 are sequentially disposed in the buffer reactor shell 15 from top to bottom, each section of heat exchange mixing unit includes a heat exchange mixing element 18, a filler 19, a filler support plate 20 for supporting the filler 19, and a filler press plate 21 for pressing the filler 19, and the filler 19 is loaded in a gap between the buffer reactor shell 15 and the heat exchange mixing element 18. The packing support plate 20 may be welded to the interior wall of the buffer reactor housing 15 or secured to the interior wall of the buffer reactor housing 15 by fasteners (e.g., screws, bolts). The packing pressing plate 21 is installed above the heat exchange mixing element 18 and used for pressing and fixing the packing 19, and the packing pressing plate 21 is fixed on the shell 15 of the buffer reactor through fasteners (such as screws and bolts) so as to be convenient for dismounting and mounting the packing 19 and overhauling. The packing support plate 20 and the packing press plate 21 are both of a mesh or screen structure. The packing 19 is selected from one of random packing, regular packing and woven mesh packing, the random packing comprises a metal woven mesh, pall rings and spherical packing, and the regular packing is a packing with a special shape, and comprises a corrugated plate, a silk screen, a skeleton packing and the like.

The buffer reactor housing 15 provides a flow-through passage for the reactants and products and provides space and support for the heat exchanging mixing elements 18. In this embodiment, the number of the heat exchange mixing units is two. As shown in fig. 6, the heat exchange mixing element 18 located above is composed of a plurality of heat exchange tubes wound in a staggered manner, and adjacent heat exchange tubes are arranged in a 60-120-degree interweaving manner (the angle at a position a in fig. 6-2 is 60 degrees, and the angle at a position B in fig. 6-3 is 120 degrees); the heat exchange tube is formed by bending, and the radius (R in figure 6-1) of a bent tube of the heat exchange tube is 0.5-1.75 times of the diameter. The heat exchange mixing element 18 can be selected from a single-pass structure or a double-pass structure. The heat exchange mixing element 18 located below is composed of a plurality of heat exchange tubes arranged in a matrix. The shell 15 of the buffer reactor is provided with a plurality of cooling and heating medium inlets and outlets 25 communicated with the heat exchange tubes, and in the embodiment, the number of the cooling and heating medium inlets and outlets 25 is four.

The top end of the buffer reactor shell 15 is provided with a second feeding hole 22, the bottom end of the buffer reactor shell 15 is provided with a discharging hole 23, the upper end and the lower end of the first distributor 16 are respectively connected with the second feeding hole 22 and the heat exchange mixing unit positioned above the first distributor, the upper end and the lower end of the second distributor 17 are respectively connected with the heat exchange mixing unit positioned below the second distributor and the discharging hole 23, and the first distributor 16 and the second distributor 17 can be a shower type distributor, a circular hole distributor, a static mixer type distributor, a calandria type distributor or a spiral pipe type distributor.

The shell 15 of the buffer reactor is also internally provided with temperature detection elements 24, and the temperature detection elements 24 are arranged at the second feed inlet 22, the discharge outlet 23 and the lower part of each heat exchange mixing element 18 of the buffer reactor 3 so as to monitor the temperature of the reaction materials in each stage in the buffer reactor 3 in real time.

The right end of the collecting pipe 11 is communicated with a second feeding hole 22 on the buffer reactor shell 15, and a discharging hole 23 is communicated with the product tank 4 through a pipeline.

The specific implementation process is as follows:

the reaction materials in the raw material tank 1 enter the corresponding first feeding hole 8 through respective pipelines, and because the first feeding hole 8 is communicated with the corresponding material inlet 901, the reaction materials enter the corresponding flat cavity 902 through the material inlet 901 and finally flow into the reaction tube array 10. In the process, the reaction materials are changed into films or layers from strand-shaped (columnar) so as to increase the contact area of the two reaction materials in the reaction tube array 10, which is beneficial to the rapid mixing and mass transfer of the reaction materials and the reaction. In addition, the baffling internals in the reaction tubes 10 change the path of the reaction materials in the reaction tubes 10, so that the reaction materials form stronger turbulence in the reaction tubes 10, the mass transfer effect is good, and the reaction is more facilitated. In the reaction process, a refrigerant flows into the shell of the microchannel rapid reactor from the cold and heat medium inlet 13, quickly absorbs heat generated by the reaction, and flows out of the shell of the microchannel rapid reactor through the cold and heat medium outlet 14, so that the quick transfer of heat is realized, the occurrence of side reactions is reduced, and the conversion rate and the yield of products are improved. In the process, as the baffle plate 12 is designed in the shell of the microchannel rapid release reactor, the refrigerant in the shell of the microchannel rapid release reactor forms stronger turbulent flow, thereby absorbing heat more rapidly.

The reaction material in the reaction tubes 10 flows toward the manifold 11 while reacting in the reaction tubes 10, and flows into the second feed inlet 22 of the buffer reactor casing 15, and then enters the buffer reactor 3. The buffer reactor 3 can increase the tube pass and mass transfer of the reaction materials, so that the reaction materials which are not completely reacted in the reaction tubes 10 are further reacted, thereby further improving the conversion rate and the yield of the product.

Specifically, before the reaction material enters the buffer reactor shell 15, the cold and heat medium enters and exits the heat exchange mixing element 18 through the cold and heat medium inlet and outlet 25 to provide a heat exchange area for the reaction material, the reaction material enters the buffer reactor shell 15 through the second feed inlet 22 at the top end of the buffer reactor shell 15, and primarily mixes raw materials through the first distributor 16 and the heat exchange mixing element 18, then the heat exchange mass transfer reaction is performed in the buffer reactor shell 15, and after the reaction is fully completed, the reaction material is discharged through the discharge outlet 23 at the bottom end of the buffer reactor shell 15 and enters the product tank 4. In the above process, the filler 19 in the shell 15 of the buffer reactor can increase the contact interface of liquid and liquid phases, and at the same time, the temperature and flow of the cooling and heating medium in the heat exchange mixing element 18 can be adjusted to realize the accurate control of the reaction temperature.

To sum up, this embodiment utilizes microchannel fast reactor 2 to realize the quick transfer of heat, effectively reduces the side reaction to utilize buffer reactor 3 to further carry out material reaction, thereby further improved the conversion, improved the yield of product.

Example two

The present embodiment is different from the first embodiment only in that: in this embodiment, the number of microdistributors 9 is two, and the number of reaction tubes is two, and two reaction tubes correspond to microdistributors 9 one-to-one to improve the throughput of microchannel rapid reactor to reaction materials.

The above embodiments are merely illustrative of the principles and effects of the present invention, and are not to be construed as limiting the invention. It will be apparent to those skilled in the art that modifications and variations can be made to the above-described embodiments without departing from the spirit and scope of the invention, and it is intended that all equivalent modifications and variations be covered by the appended claims without departing from the spirit and scope of the invention.

Claims (10)

1. A high-conversion-rate continuous flow reaction system is characterized by comprising a micro-channel rapid reactor and a buffer reactor, wherein the micro-channel rapid reactor comprises a micro-channel rapid reactor shell, a plurality of first feed inlets are formed in the micro-channel rapid reactor shell, a micro-distributor and a reaction pipeline are arranged in the micro-channel rapid reactor shell, a plurality of material inlets and a plurality of flat cavities communicated with corresponding material inlets are formed in the micro-distributor, the material inlets are communicated with the corresponding first feed inlets, one ends, far away from the material inlets, of the flat cavities are communicated with the reaction pipeline, and a cold and hot medium inlet and a cold and hot medium outlet are formed in the micro-channel rapid reactor shell; the buffer reactor comprises a buffer reactor shell, a plurality of sections of heat exchange mixing units are arranged in the buffer reactor shell, each section of heat exchange mixing unit comprises a heat exchange mixing element, each heat exchange mixing element consists of a plurality of staggered and coiled heat exchange tubes or a plurality of heat exchange tubes arranged in a matrix, and a plurality of cold and heat medium inlets and outlets communicated with the heat exchange tubes are arranged on the buffer reactor shell; and a second feeding hole and a second discharging hole are formed in the shell of the buffer reactor, and one end, far away from the micro distributor, of the reaction pipeline is communicated with the second feeding hole in the shell of the buffer reactor.

2. The high conversion continuous flow reaction system of claim 1, wherein the microchannel rapid reactor housing is provided with baffles for obstructing flow of the heating and cooling medium.

3. The high conversion continuous flow reaction system of claim 1, wherein the inner wall of the reaction tube is provided with a plurality of baffle internals for obstructing the flow of the material.

4. The high-conversion continuous-flow reaction system of claim 1, wherein the number of the micro-distributors is two or more, the number of the reaction pipes is the same as that of the micro-distributors, the reaction pipes correspond to the micro-distributors one by one, and one ends of the reaction pipes far away from the micro-distributors are communicated with the second feed inlet on the shell of the buffer reactor through the collecting pipe.

5. The high conversion continuous-flow reaction system of claim 1, wherein the heat exchange mixing unit further comprises a packing material loaded in the gap between the buffer reactor shell and the heat exchange mixing element.

6. The high conversion continuous-flow reaction system of claim 2, wherein the heat exchange mixing unit further comprises a packing support plate for supporting the packing and a packing press plate for compressing the packing, and the packing support plate and the packing press plate are both of a mesh or screen structure.

7. The high conversion continuous flow reaction system of claim 1, wherein a first distributor and a second distributor are disposed in the buffer reactor housing, the first distributor is connected to the second inlet and the heat exchange mixing unit near the second inlet, and the second distributor is connected to the second outlet and the heat exchange mixing unit near the outlet.

8. The high conversion continuous flow reaction system of claim 1, wherein a temperature sensing element is further disposed within the buffer reactor housing.

9. The high conversion continuous-flow reaction system of claim 1, wherein adjacent heat exchange tubes are interleaved at 60 ° to 120 °.

10. The high conversion continuous flow reaction system of claim 1, wherein the reaction conduit comprises a plurality of reaction tubes, and two adjacent reaction tubes are connected by a U-shaped tube.

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