Efficient reactor for producing chloroethane

Abstract

The invention discloses an efficient reactor for producing chloroethane, and belongs to the field of reactors, the efficient reactor comprises a shell, the shell is divided into a lower kettle type reaction zone for gas phase materials to enter and an upper tower type separation zone for liquid phase materials to enter, the lower kettle type reaction zone is internally provided with two layers of first filler which are arranged at intervals, and the upper tower type separation zone is internally provided with two layers of second filler which are arranged at intervals; three layers of fillers II which are arranged at intervals are mounted in the upper tower-type separation area, a first feeding hole, a third feeding hole and a fourth feeding hole are sequentially distributed in the lower kettle-type reaction area from bottom to top, and a fifth feeding hole is formed in the upper tower-type separation area; the interior of the reactor is divided into a lower kettle type reaction area and an upper tower type separation area, the reaction area and the separation area are filled with filler, gas and liquid phase feed ports are provided with fishbone distributors, the opening directions are different, gas and liquid phase countercurrent sufficient contact is fully guaranteed, and the efficiency of producing chloroethane through a gas-liquid method can be greatly improved.

Description

Technical Field

[0001] The invention relates to the field of reactors, in particular to a high-efficiency reactor for producing ethyl chloride. Background Art

[0002] Ethyl chloride is mainly used in the synthesis of dye intermediates, fragrance intermediates, ethyl cellulose, antibacterial agents and pesticides, and has a very wide range of uses. At present, the synthesis of ethyl chloride comes from the ethanol-hydrochloric acid or ethanol-hydrogen chloride method, accounting for more than 80% of the total market. Domestically, ethyl chloride is mainly synthesized using hydrochloric acid and ethanol at a reaction temperature of 110~145℃ and anhydrous zinc chloride as a catalyst. The reactor under this process is mostly a container reactor. Liquid materials, catalysts and gas materials are introduced into the reactor for reaction. The catalyst is unevenly distributed in the reactor, the gas-liquid contact is insufficient, and the production efficiency is low. Summary of the invention

[0003] The present invention aims at the deficiencies in the prior art and provides a reactor of kettle type and tower type, wherein the lower kettle type is used as a reaction zone and the upper tower type is used as a separation zone to improve the production efficiency of ethyl chloride. In order to solve the above technical problems, the present invention is solved by the following technical solutions.

[0004] In order to achieve the above object, the present invention adopts the following technical solutions: A high-efficiency reactor for producing ethyl chloride comprises: an outer shell, wherein the outer shell is divided into a lower kettle reaction zone for gaseous materials to enter and an upper tower separation zone for liquid materials to enter, wherein two layers of fillers 1 arranged at intervals are installed in the lower kettle reaction zone, and three layers of fillers 2 arranged at intervals are installed in the upper tower separation zone, wherein a first feed port, a second feed port, a third feed port and a fourth feed port are sequentially distributed in the lower kettle reaction zone from bottom to top, and a fifth feed port is arranged on the upper tower separation zone, wherein the first feed port, the third feed port, the fourth feed port and the fifth feed port are all provided with fishbone distributors, wherein the fishbone distributor of the first feed port and the fishbone distributors of the third feed port, the fourth feed port and the fifth feed port have different opening directions, wherein a first discharge port is arranged at the top end of the upper tower separation zone, and a second discharge port is arranged at the bottom end of the lower kettle reaction zone.

[0005] Preferably, the filler 1 and the filler 2 are selected as corrugated ceramic fillers, and the filler type is selected as corrugated ceramic filler 125Y.

[0006] Preferably, the filler 1 and the filler 2 are composed of a plurality of filler units having the same geometric shape.

[0007] Preferably, a vortex baffle is provided at the second discharge port.

[0008] Preferably, a liquid catcher 1 is provided at the contact portion between the lower kettle reaction zone and the upper tower separation zone, and a liquid catcher 2 is provided at the top of the upper tower separation zone. Both the liquid catcher 1 and the liquid catcher 2 are trough-type catchers.

[0009] Preferably, the fishbone distributor of the first feed port has an opening diameter of 8 mm, 160 openings, and an opening direction that is 45° upward.

[0010] Preferably, the second feed inlet is a catalyst inlet.

[0011] Preferably, the fishbone distributor at the third feed port has an opening diameter of 8 mm, 48 openings, and the opening direction is downward.

[0012] Preferably, the fishbone distributor of the fourth feed port has an opening diameter of 12 mm, 116 openings, and the opening direction is downward.

[0013] Preferably, the fishbone distributor of the fifth feed port has a hole diameter of 6 mm, 18 holes, and a downward direction.

[0014] Compared with the prior art, the present invention has the following beneficial effects: Compared with the existing ethyl chloride reactor, the present reactor adds an upper tower separation zone, and at the same time, corrugated ceramic filler 1 and filler 2 are respectively installed in the lower reaction zone and the upper tower separation zone, so as to increase the contact area between the gas-liquid phase and the catalyst and improve the conversion rate of the reaction; several liquid phase and gas phase feed ports are arranged in the form of fishbone distributors, holes are opened according to the flow rate, and the gas-liquid phases are fully contacted in countercurrent in the opening direction; a trough-type liquid receiving tank is added at the contact part between the lower kettle reaction zone and the upper tower separation zone and the tower top, and the condensed liquid is collected in the tank, and then flows into the reactor evenly through the small holes in the tank, so as to improve the production efficiency of ethyl chloride and effectively reduce the risk of explosion. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0016] Figure 1 Schematic diagram of the reactor of the present invention.

[0017] Explanation of the figure numbers: 1. Shell; 2. First feed port; 3. Second feed port; 4. Third feed port; 5. Fourth feed port; 6. Fifth feed port; 7. First discharge port; 8. Second discharge port; 9. Packing 1; 10. Liquid catcher 1; 11. Lower kettle reaction zone; 12. Upper tower separation zone; 13. Packing 2; 14. Vortex baffle; 15. Liquid catcher 2. DETAILED DESCRIPTION

[0018] The present invention is further described in detail below with reference to the accompanying drawings.

[0019] The following description is used to disclose the present invention so that those skilled in the art can implement the present invention. The preferred embodiments described below are only examples, and those skilled in the art can think of other obvious variations. The basic principles of the present invention defined in the following description can be used for other embodiments, variations, improvements, equivalents, and other technical solutions that do not deviate from the spirit and scope of the present invention.

[0020] Those skilled in the art should understand that, in the disclosure of the present invention, the directions or positions indicated by the terms "longitudinal", "lateral", "up", "down", "left", "right", "front", "back", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc. are based on the directions or positional relationships shown in the accompanying drawings, which are only simplified descriptions for the convenience of describing the present invention, and do not indicate or imply that the device or component referred to must have a specific direction, be constructed and operated in a specific direction. Therefore, the above terms should not be understood as limitations on the present invention.

[0021] It is to be understood that the term "one" should be understood as "at least one" or "one or more", that is, in one embodiment, the number of an element may be one, while in another embodiment, the number of the element may be multiple, and the term "one" should not be understood as a limitation on the quantity.

[0022] See also Figure 1A high-efficiency reactor for producing ethyl chloride comprises: a shell 1, the shell 1 is divided into a lower kettle reaction zone 11 for gas-phase materials to enter and an upper tower separation zone 12 for liquid-phase materials to enter, the lower kettle reaction zone 11 is provided with two-layer fillers 9 arranged at intervals, the upper tower separation zone 12 is provided with three-layer fillers 13 arranged at intervals, the fillers 1 9 and 13 are selected as corrugated ceramic fillers, the types of the fillers 1 9 and 13 are selected as corrugated ceramic fillers (125Y), the ceramic corrugated fillers are a new type of regular fillers, the fillers 1 9 and 13 are composed of many filler units with the same geometric shape; due to the structure of the ceramic, it has good hydrophilicity, the turbulence of a very thin liquid film can be formed on its surface, and the inclined and tortuous channels of the airflow can promote the airflow but not block the airflow, so that the ceramic fillers can compete with metal fillers, while the corrosion resistance and high temperature resistance of the ceramic fillers are incomparable to those of metal fillers. The surface structure has good wettability, which can accelerate the flow of liquid and reduce the amount of liquid stagnation in the filler to a minimum, thereby reducing the chances of overheating, polymerization and coking. At the same time, it increases the contact area between catalyst dispersion and gas-liquid.

[0023] The lower kettle reaction zone 11 is provided with a first feed port 2, a second feed port 3, a third feed port 4 and a fourth feed port 5 from bottom to top, and a fifth feed port 6 is provided on the upper tower separation zone 12. The first feed port 2, the third feed port 4, the fourth feed port 5 and the fifth feed port 6 are all equipped with fishbone distributors. The fishbone distributor of the first feed port 2 and the fishbone distributors of the third feed port 4, the fourth feed port 5 and the fifth feed port 6 have different opening directions. A first discharge port 7 is provided at the top end of the upper tower separation zone, and a second discharge port 8 is provided at the bottom end of the lower kettle reaction zone 11. The raw gas phase enters from the third feed port 4, the fishbone distributor at the third feed port 4 has an opening diameter of 8mm, 48 openings, and the opening direction is downward. The second feed port 3 is the catalyst inlet. The recycled gas enters from the first feed port 2 at the bottom. The fishbone distributor of the first feed port 2 has an opening diameter of 8mm, 160 openings, and the opening direction is 45° upward. The tower circulation enters from the fourth feed port 5. The fishbone distributor of the fourth feed port 5 has an opening diameter of 12mm and a number of openings. The upper tower reflux enters from the fifth feed port 6. The fishbone distributor of the fifth feed port 6 has a hole diameter of 6 mm, 18 holes, and a hole direction downward. The gas-phase material enters from the lower part of the reactor as a whole. The distributor opening faces upward, and the liquid-phase material enters from the upper part. The fishbone distributor opening faces downward, realizing gas-liquid convection and more complete contact, and also preventing a large amount of material from directly rushing into the packing 1 9 and the packing 2 13, protecting the integrity of the packing 1 9 and the packing 2 13. The opening directions of the fishbone distributor are different, which fully ensures that the gas-liquid phase countercurrent is fully contacted, which can greatly improve the efficiency of the gas-liquid method of producing ethyl chloride.

[0024] A liquid catcher 10 is provided at the contact portion between the lower kettle reaction zone 11 and the upper tower separation zone 12, and a liquid catcher 2 15 is provided at the top of the upper tower separation zone 12. Both the liquid catcher 10 and the liquid catcher 2 15 are trough-type catchers. The liquid is collected in the catcher and flows evenly into the reaction system along the holes in the trough. By adding filler 1 9 and filler 2 13, the catalyst in the reaction system can be evenly distributed in the filler 1 9 and filler 2 13, so that the reaction is more sufficient and uniform, and it is not easy to cause local reaction and explosion, thereby improving the production efficiency of ethyl chloride; a vortex baffle 14 is provided at the second discharge port 8 to prevent the recycled gas from affecting the discharge of the tower kettle when entering the reactor, resulting in insufficient pump feed.

[0025] Those skilled in the art should understand that the embodiments of the present invention described above and shown in the accompanying drawings are only examples and do not limit the present invention. The purpose of the present invention has been fully and effectively achieved. The functions and structural principles of the present invention have been demonstrated and explained in the embodiments, and the embodiments of the present invention may be changed or modified without departing from the principles.

Claims

1. A high efficiency reactor for producing ethyl chloride, characterized in that: include: The outer shell (1) is divided into a lower kettle reaction zone (11) for gaseous materials to enter and an upper tower separation zone (12) for liquid materials to enter. The lower kettle reaction zone (11) is provided with two layers of filler 1 (9) arranged at intervals. The upper tower separation zone (12) is provided with three layers of filler 2 (13) arranged at intervals. The lower kettle reaction zone (11) is provided with a first feed inlet (2), a second feed inlet (3), a third feed inlet (4) and a fourth feed inlet (5) in sequence from bottom to top. A fifth feed port is provided on the tower separation zone (12); fishbone distributors are installed at the first feed port (2), the third feed port (4), the fourth feed port (5) and the fifth feed port (6); the fishbone distributor of the first feed port (2) and the fishbone distributors of the third feed port (4), the fourth feed port (5) and the fifth feed port (6) have different opening directions; a first discharge port (7) is provided at the top end of the upper tower separation zone (12); and a second discharge port (8) is provided at the bottom end of the lower kettle reaction zone (11).

2. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The packing 1 (9) and the packing 2 (13) are selected to be corrugated ceramic packings.

3. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The filler material 1 (9) and the filler material 2 (13) are composed of a plurality of filler units having the same geometric shape.

4. A high-efficiency reactor for producing ethyl chloride according to claim 3, characterized in that: A vortex baffle (14) is provided at the second discharge port (8).

5. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: A liquid catcher 1 (10) is provided at the contact portion between the lower kettle reaction zone (11) and the upper tower separation zone (12), and a liquid catcher 2 (15) is provided at the top of the upper tower separation zone (12).

6. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The fishbone distributor of the first feed port (2) has an opening diameter of 8 mm, 160 openings, and an opening direction that is 45° upward.

7. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The second feed port (3) is a catalyst inlet.

8. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The fishbone distributor at the third feed port (4) has an opening diameter of 8 mm, a number of openings of 48, and an opening direction downward.

9. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The fishbone distributor of the fourth feed port (5) has a hole diameter of 12 mm, 116 holes, and a downward direction.

10. A high-efficiency reactor for producing ethyl chloride according to claim 1, characterized in that: The fishbone distributor of the fifth feed port (6) has a hole diameter of 6 mm, 18 holes, and the hole direction is downward.

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