Chloroethane production equipment and method for improving catalytic efficiency

Abstract

The invention discloses chloroethane production equipment and a method for improving catalytic efficiency, and belongs to the field of chloroethane production equipment.The chloroethane production equipment comprises a reactor, the reactor comprises a separation zone on the upper side and a reaction zone on the lower side, three layers of first filler are arranged in the separation zone at intervals, and two layers of second filler are arranged in the reaction zone at intervals; an ethylene and hydrogen chloride mixed gas inlet is formed in the reaction zone, and a liquid phase reflux inlet I and a liquid phase reflux inlet II with downward outlets are respectively formed in the middle upper part of the separation zone. And the proportion of adhesion of the catalyst on the filler and gas phase loss from the top of the reactor is obviously reduced.

Description

Technical Field

[0001] The present invention relates to the field of ethyl chloride production equipment, and in particular to ethyl chloride production equipment and a method for improving catalytic efficiency. Background Art

[0002] Ethyl chloride is currently mainly derived from by-product recovery and synthesis. The recovered ethyl chloride mainly comes from the by-products of synthesizing trichloroacetaldehyde and diethyl phosphite, and the synthetic ethyl chloride comes from the reaction of ethanol with hydrochloric acid or hydrogen chloride, which are the main sources of ethyl chloride in my country. At present, the domestic gas phase ethylene-hydrogen chloride process is used to produce ethyl chloride. During the operation of this process, part of the catalyst will gradually adhere to the packing or flow from the top of the reactor with the gas phase, resulting in a decrease in the catalyst concentration in the reactor system, thereby reducing the reaction efficiency and affecting the product yield. Summary of the invention

[0003] The present invention aims at the deficiencies in the prior art, provides reflux port 1 and reflux port 2 for maintaining the balance of the liquid level at the bottom of the reactor, and also plays a role in washing the ferric chloride catalyst in the gas phase of the upper packing section to prevent the catalyst from entering the condensation system. 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 chloroethane production device and a method for improving catalytic efficiency, comprising a reactor, wherein the reactor comprises a separation zone on the upper side and a reaction zone on the lower side, wherein three layers of filler 1 are arranged at intervals in the separation zone, and two layers of filler 2 are arranged at intervals in the reaction zone, an ethylene and hydrogen chloride mixed gas inlet is arranged on the reaction zone, and a liquid phase reflux port 1 and a reflux port 2 with downward outlets are respectively arranged in the upper middle portion of the separation zone.

[0005] Preferably, the first filler 1 and the second filler 1 from top to bottom correspond to reflux port 1 and reflux port 2 respectively.

[0006] Preferably, a circulation inlet for hydrogen chloride returned by a compressor is provided at the bottom of the reaction zone.

[0007] Preferably, a chloroethane forced circulation system is provided at the bottom of the reactor, the inlet of the forced circulation system is connected to the bottom of the reactor, and the outlet of the forced circulation system is connected to the upper part of the reaction zone.

[0008] Preferably, the outlet of the forced circulation system is located above the uppermost filler 2 in the reaction zone.

[0009] Preferably, the gas inlet includes an air inlet 1 and an air inlet 2 with outlets facing downward, and the air inlet 1 and the air inlet 2 are respectively located at the upper and lower sides of the lowermost filler 2.

[0010] Preferably, a catalyst inlet pipe is provided at the lower side of the reactor.

[0011] Compared with the prior art, the present invention has the following beneficial effects: The invention mainly optimizes the packing type inside the reactor and the convection distribution form of the gas-liquid phase feed inside the reactor, thereby significantly reducing the proportion of the catalyst adhering to the packing and losing from the gas phase at the top of the reactor, and can better control the concentration of the catalyst in the reaction system to ensure the reaction conversion efficiency. The reflux port 1 and the reflux port 2 are arranged to maintain the balance of the liquid level at the bottom of the reactor, and the upper packing section also plays a role in washing the ferric chloride catalyst in the gas phase, thereby preventing the catalyst from entering the condensation system. The forced circulation system increases liquid flow, making the catalyst more evenly distributed in the liquid phase system of the reactor, thereby improving the reaction effect. A heat exchanger is provided on the forced circulation system, and the heat generated by the reaction is taken away by the heat exchanger on the forced circulation system to ensure a stable reaction process. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the drawings required for use in the embodiments will be briefly introduced below. 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.

[0013] Figure 1 It is a schematic diagram of the overall structure of the present invention.

[0014] Explanation of figure numbers: 1. Reactor; 11. Separation zone; 12. Reaction zone; 2. Packing 1; 3. Packing 2; 4. Forced circulation pump; 5. Heat exchanger; 6. Gas inlet; 61. Air inlet 1; 62. Air inlet 2; 7. Reflux port 1; 8. Reflux port 2; 9. Circulation inlet. DETAILED DESCRIPTION

[0015] The present invention is further described in detail below with reference to the accompanying drawings.

[0016] 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.

[0017] 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.

[0018] 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.

[0019] See also Figure 1 A chloroethane production device and a method for improving catalytic efficiency, comprising a reactor 1, wherein the ethylene and hydrogen chloride mixed gas is first replaced with hydrogen chloride to replace nitrogen in the reactor 1 before entering the reactor 1, and then chloroethane is added to the reactor 1, wherein the reactor 1 comprises a separation zone 11 on the upper side and a reaction zone 12 on the lower side, wherein three layers of fillers 1 2 are arranged in the separation zone 11, and two layers of fillers 2 3 are arranged in the reaction zone 12, wherein the types of fillers 1 2 and 2 3 are selected as corrugated ceramic fillers 125Y, wherein the ceramic corrugated fillers are composed of a plurality of filler units having the same geometric shape, and due to the structure of the ceramic, have good hydrophilic properties, and the turbulence of a very thin liquid film and the inclined and tortuous channels of the airflow can promote the airflow without blocking 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. The reaction zone 12 is provided with an ethylene and hydrogen chloride mixed gas inlet 6, and the gas inlet 6 includes an inlet 1 61 and an inlet 2 62 with the outlet facing downward. The inlet 1 61 and the inlet 2 62 are respectively located on the upper and lower sides of the lowermost filler 2 3. Before entering the reactor 1, ethylene and hydrogen chloride are first mixed in a mixer, and after mixing, enter the reactor 1 from the inlet 1 61 and the inlet 2 62, and pass through the inlet 1 61 and the inlet 2 62. 1 and the air inlet 2 62 can better distribute the gas phase in the solvent to improve the reaction efficiency. A catalyst inlet pipe is arranged at the lower side of the reactor 1. A liquid phase reflux port 1 7 and a reflux port 2 8 with outlets facing downward are arranged in the upper part of the separation zone 11. The first filler 1 2 and the second filler 2 from top to bottom correspond to the reflux port 1 7 and the reflux port 2 8 respectively. The reflux port 1 7 and the reflux port 2 8 flow ethyl chloride from the outside to maintain the balance of the liquid level at the bottom of the reactor 1, and also wash the ferric chloride catalyst in the gas phase of the upper filler 2 to prevent the catalyst from entering the condensation system.

[0020] A circulation inlet 9 for hydrogen chloride returned by a compressor is provided at the bottom of the reaction zone 12. Since hydrogen chloride exists in the reactor 1 itself, when the ethyl chloride generated by the reaction is heated to form a gas phase and leaves the reactor 1, the hydrogen chloride also leaves. The hydrogen chloride and ethyl chloride leaving the reactor 1 first pass through a condenser, and the ethyl chloride is condensed. Under the reaction conditions, hydrogen chloride will not condense. The condensed ethyl chloride enters a separation tank, a part of which is used for the reflux of reflux port 1 7 and reflux port 2 8, while the hydrogen chloride enters from the circulation inlet 9 at the bottom of the reactor 1 after being compressed by the compressor.

[0021] A chloroethane forced circulation system is provided at the bottom of the reactor 1, the inlet of the forced circulation system is connected to the bottom of the reactor 1, the outlet of the forced circulation system is connected to the upper part of the reaction zone 12, and the outlet of the forced circulation system is located on the upper side of the uppermost filler 23 of the reaction zone 12. The forced circulation system includes a forced circulation pump 4 and a heat exchanger 5. The liquid phase enters the reactor 1 from the upper part of the reaction zone 12 through the forced circulation pump 4. The forced circulation increases the liquid flow, so that the catalyst is more evenly distributed in the liquid phase system of the reactor 1, and the reaction effect is improved. A heat exchanger 5 is provided on the forced circulation system. The heat generated by the reaction is taken away by the heat exchanger 5 on the forced circulation system to ensure the stability of the reaction process.

[0022] 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 deformed or modified in any way without departing from the principles.

Claims

1. A method for producing ethyl chloride and improving catalytic efficiency, characterized in that: The reactor (1) comprises a separation zone (11) on the upper side and a reaction zone (12) on the lower side. Three layers of filler (2) are arranged in the separation zone (11) at intervals, and two layers of filler (3) are arranged in the reaction zone (12) at intervals. An ethylene and hydrogen chloride mixed gas inlet (6) is arranged on the reaction zone (12), and a liquid phase reflux port (7) and a reflux port (8) with downward outlets are respectively arranged in the upper middle portion of the separation zone (11).

2. The ethyl chloride production equipment and the method for improving catalytic efficiency according to claim 1, characterized in that: From top to bottom, the first filler 1 (2) and the second filler 1 (2) correspond to the reflux port 1 (7) and the reflux port 2 (8) respectively.

3. The ethyl chloride production equipment and the method for improving catalytic efficiency according to claim 1, characterized in that: The bottom of the reaction zone (12) is provided with a circulation inlet (9) for hydrogen chloride returned by a compressor.

4. The ethyl chloride production equipment and the method for improving catalytic efficiency according to claim 1, characterized in that: A chloroethane forced circulation system is arranged at the bottom of the reactor (1), the inlet of the forced circulation system is connected to the bottom of the reactor (1), and the outlet of the forced circulation system is connected to the upper part of the reaction zone (12).

5. The ethyl chloride production equipment and the method for improving catalytic efficiency according to claim 4, characterized in that: The outlet of the forced circulation system is located above the uppermost filler 2 (3) of the reaction zone (12).

6. The ethyl chloride production equipment and the method for improving catalytic efficiency according to claim 1, characterized in that: The gas inlet (6) comprises a first gas inlet (61) and a second gas inlet (62) with outlets facing downwards, and the first gas inlet (61) and the second gas inlet (62) are respectively located at the upper and lower sides of the second lowermost filler (3).

7. The ethyl chloride production equipment and the method for improving catalytic efficiency according to claim 1, characterized in that: A catalyst inlet pipe is arranged at the lower side of the reactor (1).

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