CN113856568A

CN113856568A - Reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde and its control method

Info

Publication number: CN113856568A
Application number: CN202111139818.8A
Authority: CN
Inventors: 陈宝良; 张建辉; 王艺瑾; 张诗晗
Original assignee: Lianhua Xinrui Beijing Technology Co ltd
Current assignee: Lianhua Xinrui Beijing Technology Co ltd
Priority date: 2021-09-28
Filing date: 2021-09-28
Publication date: 2021-12-31

Abstract

The application discloses a reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde and a control method thereof, including a reaction kettle, a lower water outlet pipe, an upper water outlet pipe, a gas-liquid mixer assembly, an upper spiral guide plate, Upper magnetic sphere layer, lower spiral baffle, catalyst layer, lower magnetic sphere layer and distributor assembly. The application has a reasonable structure and solves the problem of heat transfer generated during the reaction process. At the same time, the rear-stage reactor adopts circulating hydrogen to stably control the production pressure, so as to avoid a series of production problems caused by uneven temperature and unstable pressure, and solve the problem. The problem of unqualified products also reduces the difficulty of production process control and greatly improves the stable production of the enterprise. The gas-liquid mixer and distributor can effectively mix the materials evenly, the temperature detection measures in the tube, and the reactor separation. The method of segment cooling and hydrogen supplementation can control the temperature and pressure of the two reactors more accurately, so as to realize the stable and continuous operation of the device.

Description

Reactor for preparing 1, 3-propylene glycol by hydrogenating 3-hydroxypropionaldehyde and control method thereof

Technical Field

The application relates to the field of chemical industry, in particular to a reactor for preparing 1, 3-propylene glycol by hydrogenating 3-hydroxypropionaldehyde and a control mode thereof.

Background

The 1, 3-propylene glycol is an important organic chemical raw material, is a main raw material for producing polytrimethylene terephthalate (PTT), is mainly used for producing polymers, can also be used as a solvent, an antifreeze agent and a protective agent, the polyester is a novel high polymer material, the fiber of the polyester has the characteristics of excellent elastic recovery, fluffiness, easy dyeing and the like, and also has the advantages of inherent stain resistance, antistatic property, good color fastness and the like, and the polymer fiber has huge potential in the application fields of clothing, engineering plastics, carpets and the like, and becomes a hotspot for developing synthetic fibers internationally at present.

The related domestic reports and patent application of the hydrogenation reaction are more, and a two-stage hydrogenation method is mainly adopted. However, there are some defects in production, mainly: firstly, the reaction temperature is difficult to control, and the higher the reaction temperature is, the higher the content of the generated acetal impurities is, so that the viscosity, the chromaticity and the like of the downstream polymerization product of the 1, 3-propylene glycol are unqualified; secondly, the reaction pressure fluctuation is large and the stable control is difficult due to the adoption of the long two-stage hydrogenation operation process. Therefore, the reactor for preparing 1, 3-propylene glycol by hydrogenating 3-hydroxypropionaldehyde and a control mode thereof are provided for solving the problems.

Disclosure of Invention

In this embodiment, a reactor for preparing 1, 3-propanediol by hydrogenating 3-hydroxypropanal and a control method thereof are provided to solve the problems in the prior art.

According to an aspect of the application, a 3-

hydroxypropionaldehyde hydrogenation preparation

1, 3 propylene glycol's reactor is provided, including reation kettle, gas-liquid mixer subassembly, go up spiral guide plate, go up magnetic sphere layer, mesh baffle, spiral guide plate, catalyst layer, magnetic sphere layer and distributor subassembly down, install respectively at magnetic sphere layer and magnetic sphere layer down in the reation kettle upper and lower end, and go up and distribute respectively about between magnetic sphere layer and the lower magnetic sphere layer and go up spiral guide plate and spiral guide plate down, the mesh baffle is installed at reation kettle middle part, and the equidistance is provided with a plurality of catalyst layers between mesh baffle and last spiral guide plate and the lower spiral guide plate, the reation kettle top is through mixing pipe and the inside intercommunication each other of gas-liquid mixer subassembly one end, and the bottom is provided with the distributor subassembly in the reation kettle.

Further, the gas-liquid mixer subassembly includes circle case, tapered cover, round hole, cavity crown plate and venthole, and tapered cover is all installed at circle incasement both ends, and two tapered cover middle parts have all seted up the round hole, the cavity crown plate is located between two tapered covers, and cavity crown plate inner ring wall annular equidistance has seted up a plurality of ventholes, is located the round hole of front end and installs atomizing nozzle.

Further, circle case one end and compounding pipe other end intercommunication each other, and the circle case other end and liquid phase inlet pipe one end intercommunication each other.

Further, the interior of the cavity annular plate is communicated with one end of the gas phase feeding pipe.

Further, the distributor subassembly includes flat case, total body, divides body and outlet pipe, and flat case fixed mounting of circle is at the top in the reation kettle, and flat case top and compounding pipe one end communicate each other, and the bottom communicates each other in total body middle part and the flat case of circle, and the equidistance is installed a plurality of branch bodys on the total body, and a plurality of outlet pipes are installed to the equidistance intercommunication on the branch body.

Furthermore, catalyst layer parts are uniformly distributed between the spiral structures of the upper spiral guide plate and between the spiral structures of the lower spiral guide plate, and a plurality of temperature detectors are arranged in the catalyst layer and extend into the reaction tubes.

Further, reation kettle one side middle part upper end and lower extreme communicate respectively and install water inlet pipe and water inlet pipe under with, and reation kettle is equipped with two, and through reactant eduction tube intercommunication each other end to end between two reation kettle, 1 section and 2 sections reactors are constituteed to two reation kettle.

Furthermore, the top of one side of the reaction kettle is communicated with and arranged on the upper water outlet pipe, the upper water outlet pipe is arranged on the control valve, and the port corresponding to the upper control valve is arranged as an upper water outlet.

Further, the bottom of one side of the reaction kettle is communicated with and provided with a lower water outlet pipe, a lower control valve is arranged on the lower water outlet pipe, and a port corresponding to the lower control valve is arranged at one end of a lower water outlet.

Further, a control mode of a reactor for preparing 1, 3-propanediol by hydrogenating 3-hydroxypropionaldehyde is specifically as follows:

liquid phase materials and gas phase materials respectively enter a gas-liquid mixer assembly through a liquid phase feeding pipe and a gas phase feeding pipe, are mixed and then enter a reaction kettle through a mixing pipe, temperature and pressure detection is arranged on the mixing pipe, and the temperature and the pressure of the mixture materials are strictly monitored;

after gas-liquid mixed materials entering the reaction kettle of the section 1 are dispersed by the distributor assembly, the materials start to react to the catalyst layer, a plurality of temperature detectors are arranged in the catalyst layer and extend into the reaction tubes, the flow of circulating water at the upper section is adjusted according to the temperature of the materials in the tubes, if the heat generated by the reaction cannot be timely removed, the adjusting valve automatically switches cooling media, and the temperature of the reaction kettle is ensured to be stable by adopting chilled water for cooling;

the material reacts under the action of a catalyst in a heat exchange tube array of the reaction kettle, the heat exchange tube array is divided into an upper section and a lower section, and the flow of a cooling medium at the upper section is controlled by the temperature in a catalyst layer in the tube array at the upper section of the reaction kettle;

the lower section adopts the same arrangement, the cooling medium of the lower section is controlled by the temperature in the catalyst layer in the lower section of the reaction kettle, and the temperature in the reaction process of the whole reaction kettle can be effectively controlled by the inlet and outlet temperature of the reaction kettle of section 1 and the temperature detection in a plurality of tubes;

the 2 sections of reaction kettle control principle is the same with section reaction kettle, but cooling medium only is equipped with the circulating water, can satisfy reaction temperature's stable control, and 2 sections of reaction kettle export sets up the pressure control governing valve, can adjust whole reaction kettle's operating pressure according to 2 sections of reaction kettle top pressure detection, if reaction pressure is not enough then automatic open circulation hydrogen valve, supplementary circulation hydrogen is with stable reaction production pressure, realizes production stabilization continuous operation.

Through the above-mentioned embodiment of this application, the heat transfer problem that produces in the reaction process has been solved, back end reactor adopts circulation hydrogen to stabilize production pressure control simultaneously, thereby avoid because of a series of production problems that the reason of temperature is inhomogeneous and pressure is unstable arouses, the problem of product ineligibility has been solved, also reduce the degree of difficulty of production process control, very big improvement the production of enterprise's stabilization, through effectual with the material homogeneous mixing of gas-liquid mixer and distributor, the temperature detection measure in the shell and tube, the mode of reactor sectional type cooling and supplementary hydrogen, the temperature and the pressure of two reactors of more accurate control, thereby realize the operation of the stable serialization of device.

Drawings

In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.

FIG. 1 is a perspective view of the overall structure of one embodiment of the present application;

FIG. 2 is a cross-sectional view of the overall structure of one embodiment of the present application;

FIG. 3 is a schematic view of a distribution of the connections between reactors according to one embodiment of the present disclosure;

FIG. 4 is a schematic diagram of a gas-liquid mixer assembly according to an embodiment of the present application;

FIG. 5 is a transverse cross-sectional view of a reactor vessel coupling structure according to one embodiment of the present application;

fig. 6 is a schematic structural diagram of a distributor assembly according to an embodiment of the present application.

In the figure: 1. a reaction kettle; 2. an inlet pipe inlet; 3. a lower water inlet pipe orifice; 4. a reactant delivery tube; 5. a lower water outlet pipe; 6. a lower control valve; 7. a lower water outlet 8 and an upper water outlet pipe; 9. an upper control valve; 10. an upper water outlet; 11. a mixing pipe; 12. a gas-liquid mixer assembly; 1201. a round box; 1202. a conical cover; 1203. a circular hole; 1204. a cavity ring plate; 1205. an air outlet; 13. a liquid phase feed pipe; 14. a gas phase feed pipe; 15. an upper spiral deflector; 16. an upper magnetic sphere layer; 17. a mesh partition plate; 18. a lower spiral deflector; 19. a catalyst layer; 20. a lower magnetic sphere layer; 21. a distributor assembly; 2101. a flat round box; 2102. a main pipe body; 2103. a pipe dividing body; 2104. and (4) flowing out of the tube.

Detailed Description

In order to make the technical solutions better understood by those skilled in the art, the technical solutions in the embodiments of the present application will be clearly and completely described below with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only partial embodiments of the present application, but not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present application.

It should be noted that the terms "first," "second," and the like in the description and claims of this application and in the drawings described above are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order. It should be understood that the data so used may be interchanged under appropriate circumstances such that embodiments of the application described herein may be used. Furthermore, the terms "comprises," "comprising," and "having," and any variations thereof, are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements expressly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.

In this application, the terms "upper", "lower", "left", "right", "front", "rear", "top", "bottom", "inner", "outer", "middle", "vertical", "horizontal", "lateral", "longitudinal", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings. These terms are used primarily to better describe the present application and its embodiments, and are not used to limit the indicated devices, elements or components to a particular orientation or to be constructed and operated in a particular orientation.

Moreover, some of the above terms may be used to indicate other meanings besides the orientation or positional relationship, for example, the term "on" may also be used to indicate some kind of attachment or connection relationship in some cases. The specific meaning of these terms in this application will be understood by those of ordinary skill in the art as appropriate.

Furthermore, the terms "mounted," "disposed," "provided," "connected," and "sleeved" are to be construed broadly. For example, it may be a fixed connection, a removable connection, or a unitary construction; can be a mechanical connection, or an electrical connection; may be directly connected, or indirectly connected through intervening media, or may be in internal communication between two devices, elements or components. The specific meaning of the above terms in the present application can be understood by those of ordinary skill in the art as appropriate.

It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict.

The reactor for preparing 1, 3-propanediol by hydrogenating 3-hydroxypropionaldehyde and the control method thereof in this embodiment can be applied to chemical production, for example, the following chemical reactor with mixing function is provided in this embodiment.

The chemical reaction device with the mixing function comprises a stirring tank, a bottom plate, a supporting cylinder, a gear ring, a first gear, a motor, a stirring shaft, a transmission disc, three transmission vertical rods and three positioning shaft rods, wherein the stirring tank is vertically arranged, a tank cover is fixed at the tank opening at the top of the stirring tank through a bolt, a stirring shaft perforation is arranged at the central position of the tank cover, the lower end of the stirring shaft is rotatably inserted into the stirring tank through the stirring shaft perforation, a spiral stirring blade is fixedly arranged on the side wall of the stirring shaft positioned at the inner side of the tank cover, a spiral stirring blade is fixed on the inner side wall of the stirring tank, the spiral stirring blade and the spiral stirring blade are reversely arranged, the bottom plate is arranged below the stirring tank, the supporting cylinder is vertically arranged between the bottom plate and the stirring tank, the upper end of the supporting cylinder is rotatably connected with the central position at the bottom of the stirring tank through a bearing, and the lower end of the supporting cylinder is fixedly connected with the corresponding position of the bottom plate, the outer side wall of the stirring tank is provided with teeth along the circumferential direction, the three transmission vertical rods are round rods, the outer side walls of the three transmission vertical rods are provided with teeth along the circumferential direction, the teeth of the three transmission vertical rods are meshed with the teeth of the stirring tank, a positioning shaft lever is vertically arranged between the lower ends of the three transmission vertical rods and the bottom plate respectively, the upper end of each positioning shaft lever is rotatably connected with the central position of the lower end of the corresponding transmission vertical rod through a bearing respectively, the lower end of each positioning shaft lever is fixedly connected with the corresponding position of the bottom plate respectively, a second gear is coaxially fixed at the upper ends of the three transmission vertical rods respectively, a transmission disc is horizontally arranged above the tank cover, the central position of the lower surface of the transmission disc is fixedly connected with the upper end of the stirring shaft, the outer side wall of the transmission disc is provided with teeth along the circumferential direction, the teeth of the transmission disc are meshed with the two gears, and the inner side wall of the gear ring is provided with teeth, the gear ring is sleeved at the middle position outside the three transmission vertical rods, teeth on the inner side wall of the gear ring are meshed with the teeth on the outer side wall of the gear ring, a first gear is meshed with the teeth on the outer side wall of the gear ring, an output shaft of the motor is fixedly connected with a gear in a coaxial mode, the bottom of the motor shell is fixedly connected with the corresponding position of the bottom plate, and the motor is powered by an external power supply.

The reactor for preparing 1, 3-propanediol by hydrogenating 3-hydroxypropanal in the examples of the present application and the manner of controlling the reactor will be described below.

Referring to fig. 1-6, a reactor for preparing 1, 3-propanediol by hydrogenating 3-hydroxypropanal comprises a reaction kettle 1, a gas-liquid mixer assembly 12, an upper spiral guide plate 15, an upper magnetic sphere layer 16, a mesh partition plate 17, a lower spiral guide plate 18, a catalyst layer 19, a lower magnetic sphere layer 20 and a distributor assembly 21, wherein the upper end and the lower end of the reaction kettle 1 are respectively arranged on the magnetic sphere layer 16 and the lower magnetic sphere layer 20, an upper spiral guide plate 15 and a lower spiral guide plate 18 are respectively distributed between the upper magnetic sphere layer 16 and the lower magnetic sphere layer 20 from top to bottom, the mesh baffle 17 is arranged in the middle of the reaction kettle 1, and a plurality of catalyst layers 19 are arranged between the mesh partition plate 17 and the upper spiral guide plate 15 and the lower spiral guide plate 18 at equal intervals, the top end of the reaction kettle 1 is communicated with the interior of one end of the gas-liquid mixer assembly 12 through a mixing pipe 11, and a distributor assembly 21 is arranged at the bottom in the reaction kettle 1;

the gas-liquid mixer assembly 12 comprises a round box 1201, conical covers 1202, round holes 1203, a cavity annular plate 1204 and air outlet holes 1205, wherein the conical covers 1202 are arranged at two ends in the round box 1201, the round holes 1203 are formed in the middle parts of the two conical covers 1202, the cavity annular plate 1204 is positioned between the two conical covers 1202, the air outlet holes 1205 are annularly and equidistantly formed in the inner annular wall of the cavity annular plate 1204, atomizing nozzles are arranged in the round holes 1203 at the front ends of the cavity annular plate, one end of the round box 1201 is communicated with the other end of a mixing pipe 11, the other end of the round box 1201 is communicated with one end of a liquid phase feed pipe 13, and the inner part of the cavity annular plate 1204 is communicated with one end of a gas phase feed pipe 14;

the distributor component 21 comprises a round flat box 2101, a main pipe body 2102, branch pipe bodies 2103 and outflow pipes 2104, the round flat box 2101 is fixedly installed at the top of the inside of the reaction kettle 1, the top of the round flat box 2101 is communicated with one end of the mixing pipe 11, the middle of the main pipe body 2102 is communicated with the bottom of the inside of the round flat box 2101, the main pipe body 2102 is provided with a plurality of branch pipe bodies 2103 at equal intervals, and the branch pipe bodies 2103 are provided with a plurality of outflow pipes 2104 at equal intervals.

Catalyst layers 19 are distributed between the spiral structures of the upper spiral guide plate 15 and between the spiral structures of the lower spiral guide plate 18, and a plurality of temperature detectors are arranged in the catalyst layers 19 and extend into the reaction tubes; the upper end and the lower end of the middle part of one side of each reaction kettle 1 are respectively communicated and installed on a water inlet pipe orifice 2 and a lower water inlet pipe orifice 3, two reaction kettles 1 are arranged, the two reaction kettles 1 are communicated with each other end to end through a reactant delivery pipe 4, and the two reaction kettles 1 form a reactor 1 and a reactor 2; the top of one side of the reaction kettle 1 is communicated with and mounted on an upper water outlet pipe 8, the upper water outlet pipe 8 is mounted on a control valve 9, and an upper water outlet 10 is formed in a corresponding port of the upper control valve (9); the bottom of one side of the reaction kettle 1 is communicated with and provided with a lower water outlet pipe (5), a lower control valve 6 is arranged on the lower water outlet pipe 5, and one end of a lower water outlet 7 is arranged at the corresponding port of the lower control valve 6.

A control mode of a reactor for preparing 1, 3-propylene glycol by hydrogenating 3-hydroxypropionaldehyde is specifically as follows:

liquid phase materials and gas phase materials respectively enter a gas-liquid mixer assembly 12 through a liquid phase feeding pipe 13 and a gas phase feeding pipe 14 to be mixed, then enter the reaction kettle 1 through a mixing pipe 11, temperature and pressure detection is arranged on the mixing pipe 11, and the temperature and the pressure of the mixture materials are strictly monitored;

after gas-liquid mixed materials entering the reaction kettle 1 at the section 1 are dispersed by the distributor component 21, the materials start to react at the catalyst layer 19, a plurality of temperature detectors are arranged in the catalyst layer 19 and extend into the reaction tube array, the flow of circulating water at the upper section is adjusted according to the material temperatures in the plurality of tube arrays, if the heat generated by the reaction cannot be timely removed, the adjusting valve automatically switches cooling media, and chilled water is adopted for cooling so as to ensure the temperature of the reaction kettle 1 to be stable;

the material reacts under the action of the catalyst in the heat exchange tube array of the reaction kettle 1, the heat exchange tube array is divided into an upper section and a lower section, and the flow of the cooling medium at the upper section is controlled by the temperature in the catalyst layer 19 in the tube array at the upper section of the reaction kettle 1;

the lower section adopts the same arrangement, the cooling medium of the lower section is controlled by the temperature in the catalyst layer 19 in the lower section array pipe of the reaction kettle 1, and the temperature in the reaction process of the whole reaction kettle 1 can be effectively controlled by the inlet and outlet temperature of the reaction kettle 1 of the section 1 and the temperature detection in a plurality of array pipes;

2 section reation kettle 1 control principle is the same with 1 section reation kettle 1, but coolant only is equipped with the circulating water, can satisfy reaction temperature's stability control, 2 section reation kettle 1 exports and sets up the pressure control governing valve, can detect the operating pressure who adjusts whole reation kettle 1 according to 2 section reation kettle 1 top pressure, if reaction pressure is not enough then the automatic circulating hydrogen valve of opening, supplementary circulating hydrogen is with stable reaction production pressure, realizes production stabilization continuous operation.

The application has the advantages that:

1. the reactor has a reasonable structure, the problem of heat transfer generated in the reaction process is solved systematically by reforming the feeding mixing mode, the reaction cooling mode and the process control (temperature and pressure) of the reactor for preparing the 1, 3-propanediol by hydrogenating the 3-hydroxypropionaldehyde, and meanwhile, the back-end reactor adopts circulating hydrogen to stabilize the production pressure control, so that a series of production problems caused by uneven temperature and unstable pressure are avoided, the problem of unqualified products is solved, the difficulty in controlling the production process is reduced, and the stable production of enterprises is greatly improved;

2. this application is rational in infrastructure, through the effectual mode with material homogeneous mixing, temperature detection measure, reactor sectional type cooling and supplementary hydrogen in shell and tube of gas-liquid mixer and distributor, the temperature and the pressure of two reactors of more accurate control to realize the operation of the device stabilization serialization.

The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.

Claims

1. a reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde, is characterized in that: comprise reactor (1), gas-liquid mixer assembly (12), upper spiral deflector (15), upper A magnetic ball layer (16), a mesh baffle (17), a lower helical baffle (18), a catalyst layer (19), a lower magnetic ball layer (20) and a distributor assembly (21), the reaction kettle ( 1) The inner and upper ends are respectively installed on the magnetic sphere layer (16) and the lower magnetic sphere layer (20), and upper and lower helical baffles are respectively distributed between the upper magnetic sphere layer (16) and the lower magnetic sphere layer (20). (15) and a lower spiral baffle (18), the mesh baffle (17) is installed in the middle of the reactor (1), and the mesh baffle (17) is connected to the upper spiral baffle (15) and A plurality of catalyst layers (19) are arranged equidistantly between the lower spiral guide plates (18), and the top of the reaction kettle (1) is communicated with one end of the gas-liquid mixer assembly (12) through the mixing pipe (11). , and a distributor assembly (21) is arranged at the inner bottom of the reactor (1).

2. a kind of reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde according to claim 1, is characterized in that: described gas-liquid mixer assembly (12) comprises round box (1201), cone type A cover (1202), a circular hole (1203), a cavity ring plate (1204) and an air outlet (1205), a conical cover (1202) is installed on both ends of the circular box (1201), and the two conical covers ( 1202) A circular hole (1203) is formed in the middle part, the cavity ring plate (1204) is located between the two cone-shaped covers (1202), and the inner ring wall of the cavity ring plate (1204) has a plurality of annular equidistant openings. There are two air outlet holes (1205), and an atomizing nozzle is installed in the circular hole (1203) at the front end.

3. a kind of reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde according to claim 2, is characterized in that: one end of described round box (1201) is communicated with the other end of mixing pipe (11) , and the other end of the circular box (1201) communicates with one end of the liquid-phase feed pipe (13).

4. a kind of reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde according to claim 2, is characterized in that: the inside of described cavity ring plate (1204) and one end of gas phase feed pipe (14) interconnected.

5. a kind of reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde according to claim 1, is characterized in that: described distributor assembly (21) comprises round flat box (2101), general pipe body ( 2102), the sub-pipe body (2103) and the outflow pipe (2104), the round flat box (2101) is fixedly installed on the top of the reactor (1), and the top of the round flat box (2101) and one end of the mixing pipe (11) are communicated with each other , the middle part of the main pipe body (2102) and the inner bottom of the round flat box (2101) are connected to each other, and the main pipe body (2102) is equidistantly installed with a plurality of branch pipe bodies (2103), and the branch pipe body (2103) is equidistantly connected and installed with multiple pipe bodies (2103). an outflow tube (2104).

6. a kind of reactor for preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde according to claim 1, is characterized in that: between the helical structure of described upper helical guide plate (15) and the lower helical guide Parts of a catalyst layer (19) are distributed between the spiral structures of the flow plates (18), and a plurality of temperature detectors are arranged in the catalyst layer (19) and go deep into the reaction tube.

7. a kind of 3-hydroxypropionaldehyde hydrogenation according to claim 1 prepares the reactor of 1,3 propylene glycol, it is characterized in that: described reaction kettle (1) side middle part upper end and lower end are respectively connected and installed on the water inlet pipe The mouth (2) and the lower water inlet pipe mouth (3), and the reaction kettle (1) is provided with two, and the two reaction kettles (1) are connected with each other end to end through the reactant outlet pipe (4), and the two reaction kettles (1). 1) 1-stage and 2-stage reactors are formed.

8. a kind of 3-hydroxypropionaldehyde hydrogenation according to claim 1 prepares the reactor of 1,3 propylene glycol, it is characterized in that: described reactor (1) side top is connected and installed on upper outlet pipe (8) , and the upper water outlet pipe (8) is installed on the control valve (9), and the corresponding port of the upper control valve (9) is set as the upper water outlet (10).

9. a kind of 3-hydroxypropionaldehyde hydrogenation according to claim 1 prepares the reactor of 1,3 propylene glycol, it is characterized in that: described reactor (1) side bottom part is connected and installed with lower outlet pipe (5 ), and a lower control valve (6) is installed on the lower water outlet pipe (5), and the corresponding port of the lower control valve (6) is set as one end of the lower water outlet (7).

10. the control mode that a kind of reactor of preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde according to claim 1-9 obtains a kind of reactor of preparing 1,3 propylene glycol by hydrogenation of 3-hydroxypropionaldehyde, It is characterized in that: the control mode is specifically as follows:

The liquid-phase material and the gas-phase material respectively enter the gas-liquid mixer assembly (12) through the liquid-phase feeding pipe (13) and the gas-phase feeding pipe (14) for mixing, and then enter the reaction kettle (1) through the mixing pipe (11) , temperature and pressure detection are set on the mixing pipe (11) to strictly monitor the temperature and pressure of the mixture material;

After the gas-liquid mixture material entering the 1-stage reaction kettle (1) is dispersed by the distributor assembly (21), the reaction starts in the catalyst layer (19), and a plurality of temperature detections are arranged in the catalyst layer (19) to penetrate deep into the reaction tube, Adjust the flow rate of the circulating water in the upper section according to the temperature of the materials in the multiple tubes. If the heat produced by the reaction cannot be removed in time, the regulating valve will automatically switch the cooling medium and use chilled water for cooling to ensure a stable temperature of the reactor (1);

The material reacts under the action of the catalyst in the heat exchange tube of the reactor (1), the heat exchange tube is divided into upper and lower sections, and the flow rate of the cooling medium in the upper section is determined by the temperature in the catalyst layer (19) in the upper section of the reactor (1). to control;

The lower section adopts the same setting, and the cooling medium of the lower section is controlled by the temperature in the catalyst layer (19) in the lower section of the reactor (1), and can be detected through the inlet and outlet temperature of the first section of the reactor (1) and the temperature in the multiple tubes. Effectively controls the temperature of the entire reaction kettle (1) reaction process;

The control principle of the 2-stage reactor (1) is the same as that of the 1-stage reactor (1), but the cooling medium is only provided with circulating water, which can satisfy the stable control of the reaction temperature, and the outlet of the 2-stage reactor (1) is provided with a pressure control regulating valve. The operating pressure of the entire reactor (1) can be adjusted according to the pressure detection at the top of the 2-stage reactor (1), if the reaction pressure is insufficient, the circulating hydrogen valve will be automatically opened, and the circulating hydrogen will be supplemented to stabilize the reaction production pressure and achieve stable production and continuous operation.