Tower type reactor device

Abstract

A tower reactor device comprises a tower body, at least two tower trays are arranged in the tower body at intervals in the height direction, the upstream end of a vapor phase pipeline located on the bottom layer is used for being connected with a vapor phase material source, the upstream ends of other vapor phase pipelines extend to the tower trays on the adjacent lower layer and are located above the liquid level, and the downstream ends of the vapor phase pipelines extend to the corresponding tower trays. The upstream end of the downcomer pipeline is located below the liquid level and extends to the adjacent upper-layer tower tray, the downstream end of the downcomer pipeline is located below the liquid level and extends to the corresponding tower tray, the upstream end of the first pipeline is connected with a pressure source through a pressure tank, the first pipeline is provided with a plurality of first branch pipelines and extends to the corresponding tower trays, and each first branch pipeline is provided with a third valve; the downstream end of the second pipeline is connected with the pressure tank, a plurality of second branch pipelines are arranged on the second pipeline, extend to the corresponding trays and are positioned below the liquid level, and fourth valves are arranged on the second branch pipelines. According to the utility model, the catalyst can be replaced and the tray can be maintained without shutdown.

Description

TECHNICAL FIELD

[0001] The utility model relates to the field of chemical industry, especially relates to a tower type reactor device. BACKGROUND

[0002] The tower type reactor is a kind of reactor widely used in liquid phase participation's medium speed, slow reaction and the reactor of big heat release.

[0003] For tower tray type reactor, liquid phase material is generally entered from the top of tower body, flows downwards in each tray, low-boiling point material is vaporized and entered from the bottom of tower body, and gradually diffuses upwards, and target product is generated by reaction, and generally, catalyst is arranged in each tray.

[0004] With the reaction, catalyst is gradually deactivated, and waste catalyst must be removed and replaced with fresh catalyst, generally, this needs to stop, seriously affects production progress, and the cost of stop and start is higher.In addition, the damage or failure of single tray will also cause the reactor to stop for repair, which cannot meet the production needs of enterprises.

[0005] Therefore, designing a tower type reactor for replacing catalyst without stopping and long-time production is an urgent problem for those skilled in the art to solve. SUMMARY

[0006] The utility model aims at the deficiency of prior art, provides a tower type reactor device, which is simple in structure, convenient to operate, can replace catalyst without stopping, maintain tray without stopping, and meets the production needs of enterprises.

[0007] The utility model discloses a technical scheme is: a tower reactor device, including tower body, first pipeline, second pipeline and multiple vapor phase pipelines, multiple liquid downcomer, the top of tower body sets up liquid inlet, and the bottom sets up discharge port, at least two trays are arranged along the height direction in the interval in the tower body, and the internal space of tower body is divided into a plurality of independent spaces, the number of vapor phase pipeline is adapted to the number of tray, and the upstream end of each vapor phase pipeline is provided with first valve, and the upstream end of vapor phase pipeline in the bottom layer is used for connecting with vapor phase material source, the upstream end of remaining vapor phase pipeline extends to the tray of adjacent lower layer, and is located above liquid level, and the downstream end of each vapor phase pipeline is provided with second valve, and extends to the corresponding tray, and is located below liquid level, the upstream end of liquid downcomer extends to the tray of adjacent upper layer, and is located below liquid level, and the downstream end extends to the corresponding tray, the upstream end of first pipeline is connected with pressure source through pressure tank, and the downstream end is sealed, and a plurality of first branch pipelines are arranged on first pipeline and extend to the corresponding tray, and third valve is arranged on each first branch pipeline, the upstream end of second pipeline is sealed, and the downstream end is connected with pressure tank, and a plurality of second branch pipelines are arranged on second pipeline and extend to the corresponding tray and are located below liquid level, and fourth valve is arranged on each second branch pipeline.

[0008] Still include a plurality of pressure balance pipelines, one end of pressure balance pipeline is connected with corresponding liquid downcomer, and the other end extends to the corresponding tray and is located above liquid level.

[0009] The upstream end of vapor phase pipeline in the bottom layer is connected with heater.

[0010] Emergency pipeline is connected between two adjacent vapor phase pipelines, and fifth valve is arranged, and the connecting position of emergency pipeline and vapor phase pipeline is located between first valve and second valve.

[0011] The pressure source is nitrogen source.

[0012] The downstream end of second pipeline is provided with sixth valve.

[0013] The downstream end of each first branch pipeline is connected on corresponding second branch pipeline and is located between fourth valve and tray.

[0014] Overflow section is arranged on the pipe section of each liquid downcomer, and the height is higher than the downstream end of corresponding second branch pipeline.

[0015] The above technical scheme has the following beneficial effects:

[0016] 1. The tower reactor device comprises a tower body, a first pipeline, a second pipeline, a plurality of vapor phase pipelines and a plurality of downcomers. The tower body is provided with a liquid inlet at the top and a discharge port at the bottom, and is used to provide a reaction space. Liquid raw materials enter the tower body through the liquid inlet at the top, and the reacted materials are discharged through the discharge port at the bottom. At least two trays are arranged in the tower body along the height direction, which divides the internal space of the tower body into a plurality of independent spaces, i.e. each tray serves as an independent reaction space, and the trays can be loaded with catalysts. The number of vapor phase pipelines is adapted to the number of trays. The upstream end of each vapor phase pipeline is provided with a first valve. The upstream end of the vapor phase pipeline at the bottom is connected to a vapor phase material source, and the upstream end of the remaining vapor phase pipeline extends to the tray of the adjacent lower layer and is located above the liquid level. The downstream end of each vapor phase pipeline is provided with a second valve and extends to the corresponding tray and is located below the liquid level. After the vapor phase material or liquid phase material is vaporized into a vapor phase, it enters the bottom tray through the vapor phase pipeline at the bottom and reacts with the liquid raw material as a raw material. Excess vapor phase raw material enters the upper tray through the upper vapor phase pipeline and reacts with the liquid raw material as a raw material, ensuring material utilization and reaction efficiency. The upstream end of the downcomer extends to the tray of the adjacent upper layer and is located below the liquid level. The downstream end extends to the corresponding tray. The reaction material of the upper tray enters the lower tray through the downcomer and reacts with the vapor phase raw material as a raw material, ensuring material utilization and reaction efficiency. The upstream end of the first pipeline is connected to a pressure source through a pressure tank, and the downstream end is sealed. A plurality of first branch pipelines are arranged on the first pipeline and extend to the corresponding tray. A third valve is arranged on each first branch pipeline. The catalyst can be added to the corresponding tray by opening the corresponding third valve through the first pipeline and pressurizing to meet the reaction conditions of the raw material. The upstream end of the second pipeline is sealed, and the downstream end is connected to a pressure tank. A plurality of second branch pipelines are arranged on the second pipeline and extend to the corresponding tray and are located below the liquid level. A fourth valve is arranged on each second branch pipeline. The catalyst can be carried into the pressure tank by opening the corresponding fourth valve and adjusting the pressure of the pressure tank to be less than the pressure in the corresponding tray, and after separation, the catalyst is supplemented in the pressure tank and pressurized to return to the corresponding tray through the first branch pipeline, realizing the production demand of replacing the catalyst without stopping.

[0017] 2. It also comprises a plurality of pressure balance pipelines. One end of the pressure balance pipeline is connected to the corresponding downcomer, and the other end extends to the corresponding tray and is located above the liquid level, which is beneficial to the smooth discharge of the materials in the tray to the lower tray through the corresponding downcomer.

[0018] 3. The upstream end of the vapor phase pipeline at the bottom is connected to a heater, which is used to vaporize low-boiling-point liquid phase materials or maintain the vapor phase raw material in a gaseous state to enter the tower body as a raw material. It also provides heat to the tower body to meet the actual production demand.

[0019] 4. The emergency pipeline is connected between two adjacent vapor phase pipelines, and a fifth valve is arranged, and the connection position of the emergency pipeline and the vapor phase pipeline is between the first valve and the second valve, when the corresponding tray does not need to supplement the vapor phase material, or the tray needs to be isolated for maintenance, the first valve and the second valve of the corresponding vapor phase pipeline can be closed, and the corresponding fifth valve is opened, so that the vapor phase material bypasses the tray and enters the higher layer tray as raw material, realizes the purpose of maintaining the tray without stopping, and meets the actual production needs of enterprises.

[0020] 5. The pipe section of each said downcomer pipeline is provided with an overflow section, and the height of the overflow section is higher than the downstream end of the corresponding second branch pipeline, so that the liquid level in the tray is higher than the height of the overflow section, and the liquid phase material can flow to the lower layer tray through the downcomer pipeline, and the fourth valve on the corresponding second branch pipeline is opened, so that the liquid phase material bypasses the tray and enters the lower layer tray as raw material, realizes the purpose of maintaining the tray without stopping, and meets the actual production needs of enterprises.

[0021] The specific embodiments are further described below in conjunction with the drawings and specific embodiments. BRIEF DESCRIPTION OF DRAWINGS

[0022] Figure 1 The connection diagram of the utility model.

[0023] In the drawings, 1 is a first pipeline, 11 is a first branch pipeline, 2 is a second pipeline, 21 is a second branch pipeline, 3 is a tower body, 31 is a liquid inlet, 32 is a discharge port, 4 is a vapor phase pipeline, 5 is a downcomer pipeline, 51 is an overflow section, 6 is a tray, 7 is a pressure tank, 8 is a pressure balance pipeline, 9 is a heater, 10 is an emergency pipeline, a is a first valve, b is a second valve, c is a third valve, d is a fourth valve, e is a fifth valve, and f is a sixth valve. DETAILED DESCRIPTION

[0024] Reference Figure 1, the first pipeline 1, the second pipeline 2, and a plurality of vapor phase pipelines 4, a plurality of downcomers 5. The tower body 3 is provided with a liquid inlet 31 at the top and a discharge port 32 at the bottom. Obviously, the liquid inlet and the discharge port are provided with valves for opening and closing. At least two trays 6 are arranged in the tower body 3 along the height direction, which divides the internal space of the tower body into a plurality of independent spaces. In this embodiment, the number of trays is four, which are uniformly distributed along the height direction of the tower body. The number of vapor phase pipelines 4 is adapted to the number of trays 6, that is, the number of vapor phase pipelines is four. The upstream end of each vapor phase pipeline 4 is provided with a first valve a. The upstream end of the vapor phase pipeline at the bottom is connected to the vapor phase material source. The upstream end of the remaining vapor phase pipeline extends to the adjacent lower tray and is located above the liquid level. In this embodiment, the upstream end of the vapor phase pipeline at the bottom is connected to a heater 9 for vaporizing the low-boiling-point liquid-phase raw material into a vapor phase as a raw material. The downstream end of each vapor phase pipeline is provided with a second valve b and extends to the corresponding tray below the liquid level. Obviously, the first valve and the second valve are located outside the tower body. In order to realize the purpose of maintaining the tray without stopping, an emergency pipeline 10 is connected between the adjacent two vapor phase pipelines, and a fifth valve e is arranged. That is, the number of emergency pipelines is three. The connection position of the emergency pipeline 10 with the vapor phase pipeline is located between the first valve a and the second valve b. The number of downcomers 5 is three. The upstream end of the downcomer extends to the adjacent upper tray below the liquid level, and the downstream end extends to the corresponding tray, which is usually above the liquid level of the corresponding tray. In order to maintain a certain liquid level height in the tray, an overflow section 51 is arranged on the pipe section of each downcomer 5. Specifically, the downcomer is a U-shaped pipe turned 90°. The upper horizontal section of the U-shaped pipe is convex upward to form an overflow section. In order to ensure the smooth flow of the liquid-phase material in the tray, three pressure balance pipelines 8 are further included. One end of the pressure balance pipeline 8 is connected to the corresponding downcomer, specifically connected to the overflow section, and the other end extends to the corresponding tray above the liquid level. The upstream end of the first pipeline 1 is connected to a pressure source through a pressure tank 7. The pressure source is a nitrogen source. The downstream end of the first pipeline 1 is sealed. Four first branch pipelines 11 are arranged on the first pipeline 1 and extend to the corresponding trays. A third valve c is arranged on each first branch pipeline. The upstream end of the second pipeline 2 is sealed, and the downstream end is connected to the pressure tank 7 and provided with a sixth valve f. Four second branch pipelines 21 are arranged on the second pipeline 2 and extend to the corresponding trays below the liquid level. A fourth valve d is arranged on each second branch pipeline 21. The downstream end of the second branch pipeline 21 is lower than the height of the overflow section 51. Specifically, the downstream end of each first branch pipeline 11 is connected to the corresponding second branch pipeline 21 and located between the fourth valve d and the tray.

[0025] The utility model discloses a working principle is: with synthetic phthalic acid di-sec -octyl ester as an example, under normal circumstances, liquid phase material phthalic acid pre -dissolved material is from the tower body liquid inlet and enters, temperature is 120 DEG C, and the flow is 8m 3 / h, and liquid phase material keeps certain liquid level in each tray and flows to the next layer tray through the corresponding liquid downpipe. The sec -octyl alcohol is vaporized after heater (180 DEG C) and is sent to the tray in the bottom layer of tower body through the bottom layer of vapor phase pipeline, and the flow is 5m 3 / h, and is heated and evaporates and flows from bottom to top through the vapor phase pipeline, and the pressure of the reaction tower bottom is 0.8Mpa. The vapor phase sec -octyl alcohol flowing upwards contacts and reacts with the phthalic acid pre -dissolved material flowing downwards, and the temperature of each tray is between 115 DEG C. A certain amount of catalyst in each tray promotes the esterification reaction, for example: p -toluene sulfonic acid, sulfuric acid, solid resin containing sulfonic acid group etc. With the fluid flowing from top to bottom along the tray, the esterification reaction gradually proceeds to the positive direction, and when the material reaches the tower bottom, the phthalic acid di-sec -octyl ester solution with content about 95% can be obtained.

[0026] When the catalyst in the tower needs to be replaced, the pressure tank is at normal pressure, the fourth valve on the second branch pipeline of the corresponding layer is opened, the liquid material in the tray of the corresponding layer carries the deactivated catalyst into the pressure tank under the action of pressure difference, after treatment, fresh catalyst is added, the fourth valve on the second branch pipeline of the corresponding layer is closed, the third valve on the first branch pipeline of the corresponding layer is opened, and the pressure tank is pressurized, the liquid material in the pressure tank carries fresh catalyst into the tray of the corresponding layer under the action of pressure difference.

[0027] When a tray needs to be maintained, taking the second layer tray as an example: the first valve and the second valve on the vapor phase pipeline of the second layer are closed, the third valve on the first layer emergency pipeline is opened, the vapor phase material of the third layer enters the first layer tray bypassing the second layer tray, the fourth valve on the second branch pipeline of the first layer is opened, and the fourth valve on the second branch pipeline of the third layer is opened, so that the liquid material in the first layer tray enters the third layer tray bypassing the second layer tray. The second layer tray is in a closed state, and the purpose of maintaining the second layer tray without stopping is realized.

Claims

1. A tower reactor apparatus characterized by: The column body (3), the first pipeline (1), the second pipeline (2), a plurality of vapor phase pipelines (4), and a plurality of downcomers (5) are included, the top of the column body (3) is provided with a liquid inlet (31), and the bottom is provided with a discharge port (32), At least two trays (6) are arranged in the column body (3) in the height direction, and the internal space of the column body is divided into a plurality of mutually independent spaces, The number of the vapor phase pipelines (4) is adapted to the number of the trays (6), the upstream end of each vapor phase pipeline (4) is provided with a first valve (a), the upstream end of the vapor phase pipeline located at the bottom layer is used to be connected with a vapor phase material source, the upstream end of the remaining vapor phase pipelines extends to the tray of the adjacent lower layer and is located above the liquid level, the downstream end of each vapor phase pipeline is provided with a second valve (b) and extends to the corresponding tray and is located below the liquid level, The upstream end of the downcomer (5) extends to the tray of the adjacent upper layer and is located below the liquid level, and the downstream end extends to the corresponding tray, The upstream end of the first pipeline (1) is connected with a pressure source through a pressure tank (7), and the downstream end is sealed, a plurality of first branch pipelines (11) are arranged on the first pipeline (1) and extend to the corresponding trays, and a third valve (c) is arranged on each first branch pipeline, The upstream end of the second pipeline (2) is sealed, and the downstream end is connected with the pressure tank (7), a plurality of second branch pipelines (21) are arranged on the second pipeline and extend to the corresponding trays and are located below the liquid level, and a fourth valve (d) is arranged on each second branch pipeline.

2. The tower reactor apparatus of claim 1, wherein: A plurality of pressure balance pipelines (8) are further included, one end of the pressure balance pipeline (8) is connected with the corresponding downcomer, and the other end extends to the corresponding tray and is located above the liquid level.

3. The tower reactor apparatus of claim 1, wherein: The upstream end of the vapor phase pipeline located at the bottom layer is connected with a heater (9).

4. The tower reactor apparatus of claim 1, wherein: An emergency pipeline (10) is connected between two adjacent vapor phase pipelines, and a fifth valve (e) is arranged, and the connection position of the emergency pipeline (10) and the vapor phase pipeline is located between the first valve (a) and the second valve (b).

5. The tower reactor apparatus of claim 1, wherein: The pressure source is a nitrogen source.

6. The tower reactor apparatus of claim 1, wherein: The downstream end of the second pipeline (2) is provided with a sixth valve (f).

7. The tower reactor apparatus of claim 1, wherein: The downstream end of each first branch pipeline (11) is connected to the corresponding second branch pipeline (21) and is located between the fourth valve (d) and the tray.

8. The tower reactor apparatus of claim 1, wherein: An overflow section (51) is arranged on the pipe section of each downcomer (5) and is higher than the height of the downstream end of the corresponding second branch pipeline (21).

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