CN215743485U

CN215743485U - Tower type temperature-changing reaction system

Info

Publication number: CN215743485U
Application number: CN202121626837.9U
Authority: CN
Inventors: 马洪玺; 吕英杰; 张文军; 孟祥立
Original assignee: Shanghai Lanke Petrochemical Engineering & Technology Co ltd
Current assignee: Shanghai Lanke Petrochemical Engineering & Technology Co ltd
Priority date: 2021-07-16
Filing date: 2021-07-16
Publication date: 2022-02-08
Anticipated expiration: 2031-07-16

Abstract

The utility model discloses a tower type variable-temperature reaction system, which comprises a reaction tower, wherein a plurality of reaction zones are arranged in the reaction tower, any reaction zone is connected with a heat exchange unit, and the heat exchange unit is provided with a heat exchange medium inflow end and a heat exchange medium discharge end; and a plurality of layers of heat exchange units are arranged in any one of the reaction zones, and adjacent heat exchange units are communicated through a flow guide pipe. Therefore, the utility model adopts a single reaction tower, a plurality of reaction zones are formed in the tower through the arrangement of the tower trays and the flow guide pipes, and each reaction zone can realize independent temperature control through the heat exchange unit, thereby realizing different temperature control requirements in the single tower.

Description

Tower type temperature-changing reaction system

Technical Field

The utility model belongs to the technical field of chemical production, and relates to a tower type temperature-changing reaction system.

Background

For the rapid reaction in the chemical field, a tubular reactor is generally adopted. For a large-scale industrial device, because reaction raw materials are more, the reaction heat release effect is large, and in order to ensure heat exchange, a single-tube reactor is replaced by a tube-type reactor so as to improve the equilibrium of the reaction. However, for a large tubular reactor, a plurality of tubular reactors need to be connected in series, resulting in large investment in a large industrial plant, increased cost and difficulty in construction.

Therefore, it is necessary for those skilled in the art to provide a temperature-variable reaction system of column type which is simple in structure, easy to be upsized, and capable of realizing different temperature control requirements.

Disclosure of Invention

The utility model aims to provide a tower type temperature-changing reaction system, which makes up the defects of the prior art and meets the requirement of accurate temperature control of large-scale reaction.

The technical scheme provided by the utility model is as follows:

a tower type temperature-changing reaction system comprises a reaction tower, wherein a plurality of reaction zones are arranged in the reaction tower, any reaction zone is connected with a heat exchange unit, and the heat exchange unit is provided with a heat exchange medium inflow end and a heat exchange medium discharge end; and a plurality of layers of heat exchange units are arranged in any one of the reaction zones, and adjacent heat exchange units are communicated through a flow guide pipe.

Preferably, the heat exchange unit comprises a tray with a hollow cavity and a stopper arranged in the vertical direction of the tray, the stopper divides the hollow cavity in the tray into a first chamber and a second chamber, one end of the stopper has a gap with the tray, so that the first chamber and the second chamber are communicated through the end gap of the stopper, and the first chamber and the second chamber are respectively communicated with the inflow end and the discharge end of the heat exchange medium; the adjacent trays are communicated through a guide pipe, so that the reaction materials flow between the trays.

Preferably, the height of the said stopper is consistent with the tray; and one end of the stopper is fixedly connected with the tray, and a gap is formed between the other end of the stopper and the tray.

Furthermore, in any layer of heat exchange unit, the tower tray is fixed on the inner wall of the reaction tower along the horizontal direction, and a guide pipe is vertically arranged at one end of the tower tray; and a gap is arranged between the lower end of the draft tube and the adjacent tray at the lower part.

Furthermore, the interval between adjacent tower trays in the reaction tower is 200-800 mm.

Further, the height of the hollow inner cavity of the tower tray is 50-100 mm.

Further, the length of honeycomb duct is 200 ~ 400 mm.

Furthermore, the height of the upper part of the tray is 50-100mm, and the length of the lower part of the tray is 100-300 mm.

Furthermore, the flow guide pipes of the adjacent trays are positioned at the two ends of the horizontal section of the tray.

Preferably, a raw material premixing feeder and a micron-sized homogenizing mixer are sequentially arranged above the heat exchange unit in the reaction tower from top to bottom; a tower kettle is arranged below the heat exchange unit in the reaction tower.

Furthermore, the raw material premixing feeder is of a conical structure, and feeding is distributed through holes on the bottom surface; the aperture ratio of the bottom surface is 30-75 percent, and the aperture of the opening is 2-10 mm.

Furthermore, the micron-sized homogenizing mixer is of a plate-type structure, tapered micropores are formed in the plate-type structure, the porosity of the plate-type structure is 4% -20%, and the pore diameter of each micropore is 20-100 microns.

Preferably, the reaction zone is set to 2-10 grades.

Preferably, the heat exchange units are all connected to a control system; and any heat exchange unit comprises a heat exchange medium inlet and outlet pipeline with a heat exchange medium control valve and a tower section temperature monitor, and the heat exchange medium control valve and the tower section temperature monitor are electrically connected with the control system.

The utility model has the following beneficial effects:

1) the utility model adopts a single reaction tower, a plurality of reaction zones are formed in the tower through the arrangement of the tower trays and the guide pipes, and each reaction zone can realize independent temperature control through the heat exchange unit, thereby realizing different temperature control requirements in the single tower. In addition, the device of the utility model can be suitable for a reaction system with the viscosity of the reaction material not more than 10cp and without a solid catalyst, and is particularly suitable for a reaction system needing temperature change control.

2) The utility model has simple structure, convenient arrangement, easy large-scale production, low investment cost and small occupied area; the investment cost of the tubular reactor is obviously reduced, and the requirement of accurate temperature control of large-scale reaction can be met.

Drawings

FIG. 1 is a schematic structural diagram of a temperature-changing reaction system of a column type according to the present invention.

Fig. 2 is an enlarged structural view of the heat exchange unit in fig. 1.

The notations in the figures have the following meanings:

1-a reaction tower; 2-a heat exchange unit; 3-a control system; 4-raw premix feeder; 5-micron level homogenizing mixer; 6-heat exchange unit, 60-tray, 61-baffle, 601-first chamber, 602-second chamber; 7-a flow guide pipe; 8-tower kettle.

Detailed Description

The technical solution of the present invention will be clearly and completely described below with reference to the specific embodiments. The following examples are only for illustrating the technical solutions of the present invention more clearly, and the protection scope of the present invention is not limited thereby.

Further, in the description of the present application, "multi-stage, multi-layer" means at least two stages, such as two stages/layers, three stages/layers, and the like, unless specifically defined otherwise.

According to an embodiment provided by the utility model, as shown in fig. 1, the system is a tower-type temperature-changing reaction system, and comprises a reaction tower 1, wherein a plurality of reaction zones are arranged in the reaction tower 1, any reaction zone is connected with a heat exchange unit 2, and the heat exchange unit 2 is provided with a heat exchange medium inflow end and a heat exchange medium discharge end; and a plurality of layers of heat exchange units 6 are arranged in any one of the reaction zones, and the adjacent heat exchange units 2 are communicated through a guide pipe 7.

According to the embodiment, a plurality of relatively independent temperature zones can be formed in the single reaction tower 1, so that the series arrangement of the tubular reactors can be replaced, the structure is simpler, and the cost is saved.

As further shown in fig. 2, the heat exchange unit 6 comprises a tray 60 with a hollow chamber, and a stopper 61 arranged along the vertical direction of the tray 60, wherein the stopper 61 divides the hollow chamber in the tray 60 into a first chamber 601 and a second chamber 602, and one end of the stopper 61 has a gap with the tray 60, so that the first chamber 601 and the second chamber 602 are communicated through the end gap of the stopper 61; and the first chamber 601 and the second chamber 602 are respectively communicated with the inflow end and the discharge end of the heat exchange medium, so that the heat exchange medium enters from one chamber, exchanges heat with the reaction material on the tray 60 and then is discharged from the other chamber, and exchanges heat with the reaction system on the tray 60. Adjacent trays 60 are communicated with each other through a draft tube 7 for the flow of the reaction fluid between the trays 60. Specifically, the height of the stopper 61 is the same as that of the tray 60, one end of the stopper 61 is fixedly connected with the tray 60, and a gap is formed between the other end of the stopper 61 and the tray, so that the flow of the heat exchange medium is promoted.

In any layer of heat exchange unit 6, the tray 60 is fixed on the inner wall of the reaction tower along the horizontal direction, and a draft tube 7 is vertically arranged at one end of the tray 60; and a gap is provided between the lower end of the draft tube 7 and the adjacent tray 60. Specifically, for the tray 60 of any layer of heat exchange unit 6, a first end of the tray in the horizontal direction is fixed on the inner wall of the reaction tower, a gap is formed between a second end of the tray and the inner wall of the reaction tower, and the draft tube 7 is vertically arranged at the second end of the tray 60. A gap for the circulation of the reaction materials is arranged between the lower end of the draft tube 7 and the adjacent tray 60, and the upper end of the draft tube 7 is higher than the upper part of the connected tray 60, so that the reaction materials can not directly fall down on the tray 60 without reaction. The arrangement of the draft tube 7 helps the reaction raw materials to fall evenly and makes the reaction more complete.

More preferably, the draft tube 7 connected to the adjacent tray 60 of the trays 60 is located at both ends of the horizontal cross section of the tray. That is, the flow guide pipes 7 between the adjacent trays 60 are arranged and communicated in a staggered manner, so that the reaction materials flow between the trays 60 in a bending manner and are fully reacted in each reaction zone.

And the first ends of adjacent trays 60 are oppositely disposed.

In order to promote the heat exchange of the reaction system and improve the accuracy of the temperature zone control, the tray 60 is preferably provided in a cylindrical shape, and the stoppers 61 are provided at the diameter of the cylindrical tray 60. In practical application, the adjacent trays 60 in the reaction tower 1 are spaced by 200-800 mm. The height of the hollow cavity in the tower tray is 50-100 mm. The length of the draft tube is 200-400 mm, wherein the length (or height) of the upper part of the tower tray is 50-100mm, and the length of the lower part of the tower tray is 100-300 mm.

In order to improve the reaction effect of the raw materials in the reaction tower, a raw material premixing feeder 4 and a micron-sized homogenizing mixer 5 are sequentially arranged above the heat exchange unit 6 in the reaction tower 1 from top to bottom. And a tower kettle 8 is arranged below the heat exchange unit 6 in the reaction tower 1.

Wherein, the raw material premixing feeder 4 is designed into a cone-shaped structure, and the feeding is distributed through holes on the bottom surface. The aperture ratio of the bottom surface is preferably 30-75%, and the aperture of the aperture is preferably 2-10 mm. The micron-sized homomixer 5 is of a plate-type structure and is provided with micropores of a conical structure, the porosity of the plate-type structure is preferably 4% -20%, and the pore diameter of the micropores is preferably 20-100 μm.

In addition, the reaction zone can be set to 2-10 grades according to the reaction requirement.

In order to further improve the reaction efficiency, the heat exchange units 2 are connected to a control system 3; any heat exchange unit 6 comprises a heat exchange medium inlet and outlet pipeline with a heat exchange medium control valve and a tower section temperature monitor, and the heat exchange medium control valve and the tower section temperature monitor are electrically connected with the control system 3. The control system 3 may adopt a common PLC or DCS control system.

Based on the above embodiment, the working principle of the utility model is as follows: reaction raw materials enter the raw material premixing feeder 4 from the feeding hole to be mixed and then are sprayed out from the bottom surface of the raw material premixing feeder 4, and then are uniformly mixed by the micron-sized homogenizer 5 and flow onto a tower tray 60 in the heat exchange unit 6 to react, and reaction heat is removed out of the system through a heat exchange medium; the heat exchange units 6 in the reaction tower 1 can be divided into 2-10 groups according to reaction heat exchange requirements, and the temperature of each heat exchange unit 6 is controlled by an independent heat exchange unit so as to adapt to the heat exchange requirements of different reaction stages; the heat exchange media of different heat exchange units can be the same or different, and the heat exchange control of each heat exchange unit 6 in the system is integrally controlled by the control system 3. The adjacent heat exchange units are communicated with the tower trays in a staggered mode through the guide pipes 7, so that the reaction fluid flows between the tower trays in a bending mode and is fully reacted in each reaction area. And finally, the reaction product after reaction flows into the tower kettle, and is discharged out of the reaction system from the bottom of the tower kettle.

It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims

1. A tower-type temperature-changing reaction system is characterized in that: the device comprises a reaction tower, wherein a plurality of stages of reaction zones are arranged in the reaction tower, any reaction zone is connected with a heat exchange unit, and the heat exchange unit is provided with a heat exchange medium inflow end and a heat exchange medium discharge end; and a plurality of layers of heat exchange units are arranged in any one of the reaction zones, and adjacent heat exchange units are communicated through a flow guide pipe.

2. The temperature-changing reaction system according to tower type of claim 1, wherein: the heat exchange unit comprises a tray with a hollow cavity and a stopper arranged in the vertical direction of the tray, the stopper divides the hollow cavity in the tray into a first cavity and a second cavity, one end of the stopper has a gap with the tray, so that the first cavity and the second cavity are communicated through the end part gap of the stopper, and the first cavity and the second cavity are respectively communicated with the inflow end and the discharge end of a heat exchange medium; the adjacent trays are communicated through a guide pipe, so that the reaction materials flow between the trays.

3. The temperature-changing reaction system according to tower type of claim 2, wherein: the height of the stoppers is consistent with that of the tower tray; and one end of the stopper is fixedly connected with the tray, and a gap is formed between the other end of the stopper and the tray.

4. The temperature-changing reaction system according to tower type of claim 2, wherein: in any layer of heat exchange unit, the tower tray is fixed on the inner wall of the reaction tower along the horizontal direction, and a guide pipe is vertically arranged at one end of the tower tray; and a gap is arranged between the lower end of the flow guide pipe and the adjacent tray.

5. The temperature-changing reaction system according to tower type of claim 4, wherein: the flow guide pipes of adjacent trays are positioned at two ends of the horizontal section of the tray.

6. The temperature-changing reaction system according to tower type of claim 1, wherein: a raw material premixing feeder and a micron-sized homogenizing mixer are sequentially arranged above the heat exchange unit in the reaction tower from top to bottom; a tower kettle is arranged below the heat exchange unit in the reaction tower.

7. The temperature-changing reaction system according to tower type of claim 6, wherein: the raw material premixing feeder is of a conical structure, and feeding is distributed through holes on the bottom surface; the aperture ratio of the bottom surface is 30-75 percent, and the aperture of the opening is 2-10 mm.

8. The temperature-changing reaction system according to tower type of claim 6, wherein: the micron-sized homogenizing mixer is of a plate type structure, tapered micropores are formed in the plate type structure, the porosity of the plate type structure is 4% -20%, and the pore diameter of each micropore is 20-100 microns.

9. The temperature-changing reaction system according to tower type of claim 1, wherein: the reaction zone is set to 2-10 grades.

10. The temperature-changing reaction system according to tower type of claim 1, wherein: the heat exchange units are all connected to a control system; and any heat exchange unit comprises a heat exchange medium inlet and outlet pipeline with a heat exchange medium control valve and a tower section temperature monitor, and the heat exchange medium control valve and the tower section temperature monitor are electrically connected with the control system.