CN210906092U

CN210906092U - Catalytic reaction system adopting fixed bed reactor

Info

Publication number: CN210906092U
Application number: CN201921922735.4U
Authority: CN
Inventors: 陈延坤; 王飞
Original assignee: Shandong Nerve Pharmaceutical Fluid System Co ltd
Current assignee: Shandong Nerve Pharmaceutical Fluid System Co ltd
Priority date: 2018-11-15
Filing date: 2019-11-08
Publication date: 2020-07-03
Anticipated expiration: 2029-11-08

Abstract

The utility model belongs to the technical field of chemical industry pharmaceutical equipment technique and specifically relates to an adopt fixed bed reactor's catalytic reaction system, a serial communication port, include: the device comprises a multistage feeding device, a multistage mixing device, a multistage preheating device, a multistage reaction device, a quenching device, a CIP cleaning device and a blowing and drying device, wherein reaction tubes in the reaction device are sequentially communicated through a baffle tube box, and the devices are controlled by means of software and a universal hardware platform according to the concentration ratio of each raw material required by chemical reaction and corresponding reaction conditions. The utility model discloses a mix effectually, reaction condition control is accurate, heat transfer misce bene, and volume and occupation of land space are less, can realize multistage chemical reaction in succession to can high-efficiently clear away the reactant in the reaction system and remain, install the solid catalysis thing in the baffling groove and catalyze the reactant, the reactant once will catalyze once through the baffling groove once, detachable solid catalysis thing is convenient for change.

Description

Catalytic reaction system adopting fixed bed reactor

Technical Field

The utility model belongs to the technical field of chemical industry pharmaceutical equipment technique and specifically relates to an adopt fixed bed reactor's catalytic reaction system.

Background

Reactor equipment commonly used in the technical field of chemical pharmacy comprises a tubular reactor, a kettle reactor and the like, wherein the kettle reactor is usually provided with a stirring device in a reaction kettle for mixing liquid-phase reactants, and the product has low purity, low reaction conversion rate and serious energy consumption and pollution. Because the chemical pharmaceutical field has high requirements on the purity and the like of products, the reactor equipment commonly used is a continuous flow tubular reactor.

The concentration and the reaction rate of chemical reactants in the tubular reactor change along with the length of the tube, so the tubular reactor needs to meet the length of the tube required by the chemical reaction, and the existing straight tube reactor or U-shaped tube reactor needs to have longer tube length, so the volume of the reactor is too large. The traditional straight tube reactor has poor turbulent effect of reaction materials and low Reynolds coefficient, and is not beneficial to heat transfer and the effect of uninterrupted mixing. In addition, the existing tubular reactor has single function, and cannot well complete reaction conditions required by chemical reaction, such as sufficient mixing, accurate temperature control, enough reaction tube length, corresponding data of on-line detection and the like required by mass transfer and heat transfer. Meanwhile, the catalyst is inconvenient to place and replace in the conventional tubular reactor, thereby catalyzing the reaction.

SUMMERY OF THE UTILITY MODEL

The utility model aims at solving the above problem, provide an adopt fixed bed reactor's catalytic reaction system to it is big to solve current tubular reaction system area, and mass transfer, heat transfer mix evenly inadequately, can't accomplish accurate accuse temperature and on-line monitoring, washs and dry, quenches and mix technical problem such as many times, installation that simultaneously can be convenient with dismantle solid catalytic substance in order to adapt to different reactions. The technical scheme is as follows:

a catalytic reaction system employing a fixed bed reactor, comprising:

the device comprises a multi-stage feeding device, a multi-stage mixing device, a multi-stage preheating device, a multi-stage reaction device, a quenching device, a CIP cleaning device and a blowing and drying device;

the feeding device, the mixing device, the preheating device and the reaction device of each stage are sequentially communicated, the first-stage mixing device is communicated with the CIP cleaning device and the blowing and drying device, the reaction device of each stage is communicated with the next-stage mixing device, and the reaction device of the last stage is communicated with the quenching device;

each stage of the feeding device comprises one or more groups of raw material tanks, a feeding pump and a flow controller which are connected in sequence, wherein each raw material tank is used for containing one reaction solution, and the flow controller is used for controlling the feeding pump to pump the reaction solution from the raw material tank at a certain speed;

each stage of the mixing device is used for mixing the reaction solution extracted from the raw material tank to obtain a mixed solution;

each stage of the preheating device comprises a preheating tube pass and a preheating shell pass, the preheating tube pass is used for circulating the mixed solution led in from the mixing device, and the preheating shell pass is used for circulating a preheating medium used for preheating reactants and preheating the mixed solution to the reaction activity critical temperature;

each stage of the reaction device comprises a reactor shell, a shell pass inlet and a shell pass outlet which are communicated with the inner cavity of the reactor shell are arranged on the reactor shell, the upper end and the lower end of the reactor shell are both connected with a tube plate and a baffle box, the baffle box is provided with a plurality of separated baffle grooves, the tube plate and the baffle groove of the baffle box jointly form a plurality of separate baffle channels, a reaction tube group is arranged in the reactor shell, the reaction tube group comprises a plurality of reaction tubes, the reaction tubes are sequentially provided with a plurality of layers from inside to outside, the upper end and the lower end of each reaction tube penetrate through and are fixedly connected to the tube plate, the adjacent reaction tubes are sequentially communicated in series one by one through the baffling channels corresponding to the reaction tubes, and a reactant inlet and a reactant outlet are arranged on the baffle box, and a solid catalytic material is arranged in the baffle groove.

On the basis of the technical scheme, the reaction tube is a straight tube or a spiral winding tube.

On the basis of the technical scheme, the CIP cleaning device comprises a plurality of raw material solvent cleaning devices and is used for replacing and cleaning different raw material solution residues in the mixing device, the preheating device and the reaction device.

On the basis of the technical scheme, the blowing and drying device comprises an inert gas generator and a gas preheater and is used for generating hot air to dry the mixing device, the preheating device and the reaction device.

On the basis of the technical scheme, a humidity detector is arranged between the reaction device at the last stage and the quenching device and is used for detecting the humidity of the gas after the sweeping and drying device is started.

On the basis of the above technical solution, the solid catalytic material occupies part or all of the cross section of the baffle tank.

On the basis of the technical scheme, the solid catalytic substance is provided with a through hole, reactant flows pass through the solid catalytic substance through the through hole, and the through hole is a large hole or consists of a plurality of small holes.

On the basis of the technical scheme, the solid catalytic substance is net-shaped.

On the basis of the technical scheme, the diversion groove is a straight groove, a wedge-shaped groove or an arc-shaped groove.

On the basis of the technical scheme, the tube plate and/or the diversion groove are/is provided with an installation groove for accommodating the solid catalytic substance, and the solid catalytic substance is installed in the installation groove.

On the basis of the technical scheme, the solid catalytic substance is arranged in the deflection groove of the upper baffle box and/or the deflection groove of the lower baffle box.

On the basis of the technical scheme, the tube plates are fixedly connected to the upper end and the lower end of the reactor shell, the reaction tubes penetrate through the tube plates and are fixedly connected with the tube plates, the tail ends of the reaction tubes are welded with the tube plates through welding points, and the tube plates are tightly attached to the baffle box through flanges and bolts.

On the basis of the technical scheme, the arrangement of the deflection grooves on the upper deflection pipe box and the lower deflection pipe box and the arrangement of the through holes on the upper tube plate and the lower tube plate ensure that the top ends and the bottom ends of the reaction tubes of each layer are arranged according to the following modes:

from outside to inside: the top ends of all the first layer of reaction tubes, namely the outermost layer of reaction tubes, are arranged to form a first upper circle, the top ends of all the second layer of reaction tubes are arranged to form a second upper circle, the second upper circle is concentric with the first upper circle, and the diameter of the second upper circle is smaller than that of the first upper circle, and so on until the last layer of reaction tubes, namely the innermost layer of reaction tubes; from outside to inside: the bottom ends of all the first layer of reaction tubes, namely the outermost layer of reaction tubes, are arranged to form a first lower circle, the bottom ends of all the second layer of reaction tubes are arranged to form a second lower circle, the second lower circle is concentric with the first lower circle, and the diameter of the second lower circle is smaller than that of the first lower circle, and so on until the last layer of reaction tubes, namely the innermost layer of reaction tubes; the upper circular circle center and the lower circular circle center are both positioned on the axial line of the reactor shell, and the included angles formed by the vertical connecting line from the top end of each reaction tube to the axial line of the reactor shell and the vertical connecting line from the bottom end of each reaction tube to the axial line of the reactor shell are equal.

All the straight line connecting lines from the top ends of the reaction tubes to the bottom ends of the reaction tubes are parallel to the axis of the reactor shell.

On the basis of the technical scheme, when the number of the reaction tubes is even, N reaction tubes are arranged, the reactant inlet and the reactant outlet are positioned on the same baffle box, the baffle grooves on the baffle box with the reactant inlet are (N/2) -1, and the baffle grooves on the other baffle box are N/2; when the number of the reaction tubes is odd, the reaction tubes are N, the reactant inlet and the reactant outlet are positioned on different baffle boxes, and the baffle grooves on the upper baffle box and the lower baffle box are (N-1)/2.

On the basis of the technical scheme, one or more online detection instruments are detachably arranged on the baffle box and are communicated with the baffle groove.

On the basis of the technical scheme, 2 spiral lines with opposite rotation directions and consistent rotation lifting angles are pressed along the outer wall of the reaction tube, so that the inner wall of the reaction tube is inwards protruded to form spiral protrusions corresponding to the two spiral lines.

The utility model has the advantages of as follows:

(1) through setting up mixing arrangement, make multiple reaction solution intensive mixing, improve reaction efficiency.

(2) Through setting up preheating device, make the reaction solution after mixing heat up before getting into reaction unit prerequisite, reach reaction temperature as early as possible after getting into reaction unit, improve reaction efficiency.

(3) Reaction unit adopts the continuous flow pipeline, and the continuous flow pipeline passes through baffle pipe case intercommunication, has reduced the distance between the adjacent reaction tube greatly, makes the length of reaction tube increase greatly in the unit volume, under the condition that satisfies same chemical reaction, the utility model discloses a volume is littleer with occupation of land space, and manufacturing cost is lower.

(4) The reaction tube is spirally wound, and reactants form spiral tangential motion along the spiral tube, so that the reactants obtain high Reynolds number under the condition of low flow velocity, the turbulent flow effect is greatly improved, and the reactants can be continuously mixed in continuous flow reaction; in addition, the whole wound reaction tube group is in a spring shape, so that the thermal stress generated by reaction heat transfer can be eliminated, the thermal stress can not be transferred to the tube plate end, and the service life of the equipment is greatly prolonged.

(5) CIP belt cleaning device with sweep drying device can high-efficiently clear away the reaction solution residue of reaction last time in the system, keep reaction system's inside clean, avoid influencing the going on of reaction next time of reaction system.

(6) The multistage feeding device, the mixing device, the preheating device and the reaction device are communicated through the continuous flow pipeline, the multistage feeding device is suitable for continuous proceeding of multistage reaction, the steps of repeated material storage and feeding are reduced, the waste heat of the previous stage reaction can be fully utilized, the production efficiency is improved, and the production cost is reduced.

(7) The detecting instrument is communicated with different baffling grooves by connecting different interfaces, so that the reaction state of reactants with different process lengths (after passing through different numbers of reaction tubes) can be detected.

(8) The baffling groove of the reaction device is internally provided with a solid catalytic substance for catalyzing reactants, the reactants can be catalyzed once when passing through the baffling groove, and the detachable solid catalytic substance is convenient to install and replace, so that the reaction device is suitable for different reactions.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below. It is obvious that the drawing in the following description is only an embodiment of the invention, and that for a person skilled in the art, other embodiments can be derived from the drawing provided without inventive effort.

FIG. 1: is a structural schematic diagram with a local section of the reaction device of the utility model (the reaction tube is a spiral winding tube);

FIG. 2: is a structural schematic diagram of the reaction tube group of the utility model;

FIG. 3: is a structural schematic diagram of the reaction tube group of the utility model after being partially cut;

FIG. 4: is a bottom view of an example of the upper baffle box of the present invention;

FIG. 5: is a top view of an example of the lower baffle box of the present invention;

FIG. 6: is a schematic structural diagram of the lower sealing gasket of the utility model;

FIG. 7: the utility model discloses a partial section structure schematic diagram of a tube plate;

FIG. 8: the partial section structure schematic diagram of the reaction tube of the utility model;

FIG. 9: the utility model discloses a partial section side view structure schematic diagram of an example of a solid catalytic substance;

FIG. 10: the utility model discloses a partial section main view structure schematic diagram of an example of the solid catalytic substance;

FIG. 11: the utility model discloses a partial section main view structure schematic diagram of an example of the solid catalytic substance;

FIG. 12: is a bottom view of an example of the upper baffle box of the present invention;

FIG. 13: the utility model discloses a partial section overlooking structure schematic diagram of an example of the solid catalytic substance;

FIG. 14: the utility model discloses a three-dimensional structure schematic diagram of an example of the solid catalytic substance;

FIG. 15: is a schematic diagram of the whole structure of the utility model;

FIG. 16: is a structural schematic diagram with a local section of the reaction device of the utility model (the reaction tube is a straight tube);

Detailed Description

The invention will be further described with reference to the following figures and examples:

reference will now be made in detail to embodiments of the present invention, examples of which are illustrated in the accompanying drawings, wherein like reference numerals refer to the same or similar elements or elements having the same or similar function throughout. The embodiments described below with reference to the drawings are exemplary only for the purpose of explaining the present invention, and should not be construed as limiting the present invention.

In the description of the present invention, it is to be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; may be directly connected or indirectly connected through an intermediate. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.

Example 1

As shown in fig. 1 to 16, a catalytic reaction system using a fixed bed reactor according to the present embodiment includes a primary feeding device 1, a primary mixing device 2, a primary preheating device 3, a primary reaction device 4, a secondary feeding device 10, a secondary mixing device 20, a secondary preheating device 30, a secondary reaction device 40, a quenching device 5, a CIP cleaning device 6, and a purging and drying device 7;

the system comprises a primary feeding device 1, a primary mixing device 2, a primary preheating device 3 and a primary reaction device 4 which are sequentially communicated, a secondary feeding device 10, a secondary mixing device 20, a secondary preheating device 30 and a secondary reaction device 40 which are sequentially communicated, a CIP cleaning device 6 and a purging and drying device 7 which are communicated with the primary mixing device 2, the primary reaction device 4 which is communicated with the secondary mixing device 20, and the secondary reaction device 40 which is communicated with a quenching device 5;

the primary feeding device 1 and the secondary feeding device 10 each comprise one or more groups of raw material tanks 100, feeding pumps 101 and flow controllers 102 connected in sequence, each raw material tank 100 is used for containing one reaction solution, and each flow controller 102 is used for controlling the feeding pump 101 to pump the reaction solution from the raw material tank 100 at a certain speed;

the primary mixing device 2 and the secondary mixing device 20 are used for mixing the reaction solution extracted from the raw material tank 100 to obtain a mixed solution;

the primary preheating device 3 and the secondary preheating device 30 both comprise a preheating tube pass 300 and a preheating shell pass 301, the preheating tube pass 300 is used for circulating the mixed solution led in from the primary mixing device 2 and the secondary mixing device 20, and the preheating shell pass 301 is used for circulating a preheating medium used for preheating reactants and preheating the mixed solution to the reaction activity critical temperature;

the first-stage reaction device 4 and the second-stage reaction device 40 both comprise a reactor shell 400, the reactor shell 400 is provided with a shell-side inlet 401 and a shell-side outlet 402 which are communicated with the inner cavity of the reactor shell 400, the upper end and the lower end of the reactor shell 400 are both connected with a tube plate 403 and a baffle box 410, the baffle box 410 is provided with a plurality of separated baffle grooves 411, the baffle grooves 411 of the tube plate 403 and the baffle box 410 jointly form a plurality of separated baffle channels, the reactor shell 400 is internally provided with a reactor tube group 41, the reactor tube group 41 comprises a plurality of reactor tubes 404, the reactor tubes 404 are sequentially provided with a plurality of layers from inside to outside, the upper end and the lower end of each reactor tube 404 are both penetrated and fixedly connected to the tube plate 403, the adjacent reactor tubes 404 are sequentially communicated in series one by one-to-one through the baffle channels corresponding to the adjacent reactor tubes 404, the baffle box 410 is provided with a reactant inlet 405 and a reactant outlet, the baffling groove 411 is internally provided with a solid catalytic material 44. The reaction tube 20 is a straight tube or a spiral wound tube.

As shown in fig. 4 and 5, the baffle box 410 is provided with a plurality of separated baffle slots 411, the tube plate 403 and the baffle slots 411 of the baffle box together form a plurality of separated baffle channels, the adjacent reaction tubes 404 in the medium flow sequence are sequentially communicated in series one by one through the corresponding baffle channels, and the baffle box 410 is provided with a reactant inlet 405 and a reactant outlet 406. That is, when the reactant inlet 405 is disposed on the lower baffle box 410, the reactant flows in the reaction tube group 41 in the order of entering the bottom end of the first reaction tube from the reactant inlet 405 on the baffle box 410, entering the first baffle box 411 of the upper baffle box 410 from the top end of the first reaction tube through the first reaction tube (the baffle box corresponds to and communicates the top end of the first reaction tube and the top end of the second reaction tube), entering the second reaction tube from the top end of the second reaction tube, entering the baffle box 411 of the lower baffle box 410 from the bottom end of the second reaction tube (the baffle box corresponds to and communicates the bottom end of the second reaction tube and the bottom end of the third reaction tube), entering the third reaction tube from the bottom end of the third reaction tube, entering the baffle box 411 of the upper baffle box 410 from the top end of the third reaction tube through the third reaction tube (the baffle box corresponds to and communicates the top end of the fourth reaction tube) Correspond to each other and connect them to each other) and then enter from the top end of the fourth reaction tube to push in this way until the reactant flows out from the reactant outlet 406. It should be noted that the first and second in this paragraph correspond to the flow sequence of the reactants, and the first reaction tube is the first reaction tube through which the reactants first flow. The utility model discloses a baffling pipe case is when using, and adjacent reaction tube is linked together through the baffling groove on the transmission direction of medium, and adjacent reaction tube need not pass through elbow or U-shaped union coupling, also need not receive the radial restriction of return bend, and the reaction tube interval is less, and the reaction unit volume is less, and the reaction flow is long.

Further, in the embodiment, a detection instrument is disposed on the baffle box 410 at the upper end of the reactor shell 400, and the detection instrument may be a temperature detection instrument 407, a pressure detection instrument 408, and a ph detection instrument 409, and is configured to measure temperature, pressure, and ph data in the reaction tube 404. The detecting instrument is connected with different interfaces and then communicated with different diversion grooves 40, so that the reaction state of reactants with different process lengths (after passing through different numbers of reaction tubes) can be detected.

Preferably, the reaction tube group 41 is composed of a plurality of reaction tubes 404 arranged in sequence from inside to outside, and the reaction tubes 404 are spirally wound tubes having a certain spiral angle, so that the reaction stroke can be further increased with the same volume.

As shown in fig. 7, preferably, the tube plates 403 are fixedly connected to the upper and lower ends of the reactor shell 400, the reaction tubes 404 pass through the tube plates 403 and are fixedly connected to the tube plates 403, and the tube plates 403 are tightly attached to the baffle boxes 410 by flanges and bolts. Further, the ends of the reaction tubes 404 are welded to the tube plate 403 by the welding points 201, so as to avoid the welding of the reaction tubes 404 and ensure the firmness and tightness of the welding.

Further, in order to ensure the tightness of the connection between the tube plate 403 and the baffle box 410, prevent the leakage of the medium in the baffle slots, and simultaneously prevent the medium from entering and flowing out of the baffle slots, a sheet-type sealing gasket 61 is arranged between the baffle box and the tube plate, and the sheet-type sealing gasket is provided with baffle holes 60 corresponding to the two ends of each baffle slot, so as to ensure the sealing of the reactant in the flowing process.

Because there are many reaction tubes which are spiral winding tubes at the same time, when installing, they are combined with the tube plate 403 and correspond to the baffle slots 411 of the baffle box 410, if there is no certain arrangement rule, it is difficult or even impossible to install, it is easy to cause the confusion of the installer, it increases the installation time and the installation error rate, so in order to install the spiral winding tubes, it is preferable that the arrangement of the baffle slots 411 on the upper and lower baffle boxes 410 and the arrangement of the through holes on the upper and lower tube plates 403 make the top and bottom of each layer of reaction tubes 404 arranged according to the following way:

from outside to inside: the top ends of all the first layer of reaction tubes 404, namely the outermost layer of reaction tubes 404, are arranged to form a first upper circle, the top ends of all the second layer of reaction tubes 404 are arranged to form a second upper circle, the second upper circle is concentric with and the diameter of the first upper circle is smaller than that of the first upper circle, and so on until the last layer of reaction tubes, namely the innermost layer of reaction tubes; from outside to inside: the bottom ends of all the first layer of reaction tubes 404, i.e. the outermost layer of reaction tubes 404, are arranged to form a first lower circle, the bottom ends of all the second layer of reaction tubes 404 are arranged to form a second lower circle, the second lower circle is concentric with the first lower circle, and the diameter of the second lower circle is smaller than that of the first lower circle, and so on until the last layer of reaction tubes, i.e. the innermost layer of reaction tubes; the upper circular circle center and the lower circular circle center are both located on the axis of the reactor shell 400, and the included angle formed by the vertical connecting line from the top end of each reaction tube belonging to the same layer to the axis of the reactor shell 400 and the vertical connecting line from the bottom end of the same reaction tube to the axis of the reactor shell 400 is equal. Further, the straight line connecting the top ends of all the reaction tubes to the bottom ends thereof (which is the line connecting the top ends and the bottom ends of the same reaction tube) is parallel to the axis of the reactor shell 400.

When the number of the reaction tubes 404 is an even number, it is assumed that the number of the reaction tubes is N, the reactant inlets 405 and the reactant outlets 406 are located on the same baffle box, the number of the baffle slots 411 on the baffle box 410 having the reactant inlets 405 is (N/2) -1, and the number of the baffle slots 411 on the other baffle box is N/2; when the number of the reaction tubes 404 is odd, it is assumed that the number is N, the reactant inlet 405 and the reactant outlet 406 are located on different baffle boxes, and the baffle slots 411 on the upper and lower baffle boxes are (N-1)/2.

As shown in fig. 8, preferably, 2 spiral lines 404a with opposite rotation directions and consistent rotation elevation angles are pressed along the outer wall of the reaction tube 404, so that the inner wall of the reaction tube is protruded inwards to form two spiral protrusions corresponding to the spiral lines. So reaction material can form great vortex when wherein flowing, and the reactant forms heliciform tangential motion along spiral arch, further improves the reynolds number that reaction material flows, improves the torrent effect greatly, improves reaction material's heat transfer and mixed effect.

Further, the CIP cleaning apparatus 6 in this embodiment includes a plurality of raw material solvent cleaning apparatuses 60 for replacing and cleaning the different raw material solution residues in the mixing apparatus, the preheating apparatus, and the reaction apparatus.

Further, the purging and drying device 7 in this embodiment includes an inert gas generator and a gas preheater for generating hot air to dry the mixing device, the preheating device, and the reaction device.

Further, a humidity detector is disposed between the secondary reaction device 40 and the quenching device 5 in this embodiment, and is used for detecting the humidity of the gas after the purging and drying device is started.

When the catalytic reaction system adopting the fixed bed reactor in this embodiment is used, the feeding device, the mixing device, the preheating device, the reaction device, the quenching device 5, the CIP cleaning device 6, and the purging and drying device 7 are controlled by software and a general hardware platform according to the concentration ratio of each raw material required by a chemical reaction and corresponding reaction conditions. The raw material solution firstly enters a primary mixing device 2 from a primary feeding device 1 according to a determined flow proportion; after the mixture is completely mixed, the mixed solution enters a primary preheating device 3 and is preheated to the critical temperature of the reaction activity; the preheated mixed solution enters a first-stage reaction device 4, and chemical reaction is fully carried out under the conditions of preset temperature, pressure and pH value to obtain a first-stage product; the primary product and the secondary raw material solution enter a secondary mixing device 20 together to be mixed, and the steps are repeated until a final product is obtained; the final product enters a quenching device 5 to obtain a cooled final product; after the reaction is finished, the CIP cleaning device 6 is controlled by software and a universal hardware platform to output raw material solvent cleaning liquid, different raw material solution residues in the mixing device, the preheating device and the reaction device are replaced and cleaned, after the cleaning is finished, the purging and drying device 7 is started again, the mixing device, the preheating device and the reaction device are dried, and the residual liquid is prevented from influencing the next chemical reaction.

The solid catalyst 44 can be fixed in the baffle 411 in the following ways:

the first fixing mode: as shown in fig. 7, the solid catalyst 44 is disposed in the cavity formed by the tube plate 403 and the diversion groove 411, and the solid catalyst 44 is in interference fit with the cavity.

And (2) fixing form II: as shown in fig. 9 and 12, a first mounting groove 46 is formed in the inner wall of the baffle 411, and a part of the solid catalyst 44 is inserted into the first mounting groove 46 and fixed in position relative to the baffle 411. The first mounting groove 46 may be formed at the bottom of the bending groove 411 or at the side wall of the first mounting groove 46, or the first mounting groove 46 may be formed at both the bottom and the side wall.

The fixed form is three: as shown in fig. 9, the tube plate 403 is formed with a second mounting groove 47 at a position corresponding to the baffle slot 411, and a part of the solid catalyst 44 is inserted into the second mounting groove 47 so as to be fixed in position relative to the baffle slot 411 and the tube plate 403.

The fixed form is four: as shown in fig. 13, the baffle 411 may be a wedge-shaped trough and the solid catalyst 44 may be a wedge-shaped block. In the diversion trench 411 of fig. 13, the flow direction of the reactants is from left to right, the solid catalyst 44 is restricted from moving to the right due to the decreasing cross-sectional area of the diversion trench 411 to the right, and the solid catalyst 44 is restricted from moving to the left due to the flow direction of the reactants.

The above fixing forms may be used alone, or a plurality of fixing forms may be combined to be used simultaneously, and fig. 9 is an example of using a plurality of fixing forms simultaneously.

The catalytic passage of the solid catalyst 44 in the baffle 411 may be in the form of:

the first channel form: as shown in fig. 7, 11, 13 and 14, the channels in the solid catalyst 44 may be a plurality of relatively small diameter through holes 45, and the reactants pass through the plurality of through holes 45 to perform catalytic reaction. Wherein, the adjacent through holes 45 can be connected by the connecting channel between the adjacent through holes 45.

Channel type two: as shown in fig. 9, the channel in the solid catalyst 44 may be a single through-hole 45 with a relatively large diameter.

The channel form III: as shown in fig. 10, there is a gap between the solid catalyst 44 and the baffle slot 411, and the gap can be used as a channel through which the reactant flows, such as the gap between the top of the solid catalyst 44 and the baffle slot 411 in fig. 10. The gap may also be provided on both sides of the solid catalyst 44.

Channel type four: as shown in fig. 10, there is a gap between the solid catalyst 44 and the tube plate 403, and the gap can be used as a channel through which the reactant flows, such as the gap between the bottom of the solid catalyst 44 and the tube plate 403 in fig. 10.

Channel type five: the solid catalyst 44 is in the form of a net having a plurality of meshes.

The above channel forms may be used alone or in combination of a plurality of channel forms to be used simultaneously, and fig. 10 and 11 are two examples of using a plurality of fixing forms simultaneously.

The solid catalyst 44 may use any combination between the above various immobilization forms and channel forms.

The solid catalyst 44 may be a bulk metal catalyst (e.g., electrolytic silver, fused iron, platinum gauze, etc.), a supported metal catalyst (e.g., Ni/Al)₂O₃Hydrogenation catalyst), alloy catalyst (active component is composed of two or more metal atoms, such as Ni-Cu alloy hydrogenation catalyst, LaNi₅Hydrogenation catalysts, etc.), and the like.

The present invention has been described above by way of example, but the present invention is not limited to the above-mentioned embodiments, and any modification or variation based on the present invention is within the scope of the present invention.

Claims

1. A catalytic reaction system employing a fixed bed reactor, comprising:

2. The catalytic reaction system according to claim 1, wherein: the reaction tube is a straight tube or a spiral winding tube.

3. The catalytic reaction system according to claim 1, wherein: the blowing and drying device comprises an inert gas generator and a gas preheater and is used for generating hot air and drying the mixing device, the preheating device and the reaction device.

4. The catalytic reaction system according to claim 1, wherein: and a humidity detector is arranged between the reaction device and the quenching device in the last stage and is used for detecting the humidity of the gas after the purging and drying device is started.

5. The catalytic reaction system using a fixed-bed reactor according to claim 1, wherein the solid catalyst occupies a part or the whole of the cross section of the baffle.

6. The catalytic reaction system using a fixed bed reactor as claimed in claim 5, wherein the solid catalyst has a through hole, and the reactant flows through the solid catalyst through the through hole, and the through hole is a large hole or is composed of a plurality of small holes.

7. The catalytic reaction system using a fixed bed reactor as set forth in claim 5, wherein said solid catalyst is in the form of a mesh.

8. The catalytic reaction system using a fixed bed reactor as set forth in claim 5, wherein said deflection groove is a straight groove, a wedge-shaped groove or an arc-shaped groove.

9. The catalytic reaction system using a fixed bed reactor as set forth in claim 5, wherein an installation groove for accommodating the solid catalyst is formed in the tube plate and/or the baffle groove, and the solid catalyst is installed in the installation groove.

10. The catalytic reaction system using a fixed bed reactor as set forth in claim 1, wherein: the solid catalytic material is arranged in the deflection tank of the upper baffle box and/or the deflection tank of the lower baffle box.