CN204816456U - A catalyst loading component - Google Patents

Abstract

The utility model relates to a catalyst loads component suitable for light petrol etherification catalyst rectification tower, should load the component and arrange in the catalyst rectification tower, including barrel and two at least column plates of setting in the barrel, be equipped with a plurality of column tray holes on the column tray, adjacent column tray constitutes the repetitive unit with the barrel, vertically be equipped with a plurality of breather pipes in the repetitive unit, the top setting of breather pipe is in the below of a column tray, its bottom is connected with another column tray, it forms porcelain ring layer and catalyst layer respectively to add porcelain ring and catalyst in proper order in the repetitive unit, the height that highly is less than the breather pipe on catalyst layer, the top of breather pipe is connected with the breather pipe cap, and the breather pipe top is opened along the junction with the breather pipe cap has a plurality of air vents. The utility model discloses catalyst filling member can improve tert carbene hydrocarbon conversion rate in the light petrol of etherification reaction process, realizes methyl tert butyl ether's effective separation, can effectively reduce the energy consumption.

Description

A catalyst loading component

technical field

The utility model relates to a catalyst filling component for a catalytic rectification tower, in particular to a catalyst filling component suitable for a light gasoline etherification catalytic distillation tower.

Background technique

The key to catalytic distillation technology lies in the structural design and installation of the catalyst bed in the reaction section. In order to meet the basic requirements of reaction and rectification, the packing method of catalyst in the tower must meet the following conditions: ① Make the catalyst bed in the reaction section have enough free space to provide a gas-liquid phase flow channel for liquid phase reaction and vapor-liquid mass transfer. ②It has enough surface area to carry out the catalytic reaction; ③It allows the expansion and contraction of the catalyst particles without damaging the catalyst.

US Pat. No. 4,471,154 proposes packing catalyst particles on trays. The upper and lower sections of the tray are separated by wire mesh, and then the tray is divided into several areas by the wire mesh, and then a certain amount of catalyst is filled in the several areas separated by the wire mesh. The advantage of this structure is that the catalyst is in a fluidized state in the wire mesh basket, the surface of the catalyst is updated quickly, and the utilization rate of the catalyst is high, but the pressure drop of the tray is large, and the loading amount of the catalyst is also limited.

U.S. Patent No. 4,215,011 proposes wrapping catalyst particles with cloth and rolling them into bundles. Use folded cloth to sew a pocket, put solid catalyst particles into the pocket, then sew the pocket, and finally roll up the bag containing the catalyst with another layer of corrugated wire mesh or steel mesh to form a cylindrical catalyst bundle, corrugated wire The voids created by the mesh allow the gas phase to pass through and contact the liquid phase for mass transfer, but the catalyst bed has a relatively high resistance.

US Patent No. 5,454,913 proposes to pack catalyst particles into the downcomer. The downcomer in the tower is made of wire mesh material, and the downcomer is directly connected from the upper part of the reaction section to the lower part, and a separation tray is designed in the middle. At the bottom of the downcomer, pipes are used to connect many downcomers and lead out of the tower through the loading and unloading port. This structure makes it easy to load and unload the catalyst, and the catalyst under the bed may be crushed.

U.S. Patent No. 5,449,501 proposes a design concept opposite to that of U.S. Patent No. 5,454,913. The downcomer is changed to a gas phase channel, and the catalyst is directly filled with the remaining space of the catalytic rectification tower. The upper and lower bottom surfaces of the catalyst bed are covered with screens to seal the catalyst.

Chinese patent CN99124796.5 makes the catalyst into particles with a central pore, connects the catalyst particles into a string with a connector, and puts it evenly into the gas and liquid free channels of the structured packing to form a catalytic rectification structure. This catalytic rectification structure has the characteristics of uniform catalyst distribution and large bed voids at the same time, so that the catalyst utilization rate is high and the tower pressure drop is small. However, the catalyst loading is small and the production process is complicated.

Chinese patent CN03265855.9 proposes to pack catalyst particles into a mesh bag, and the mesh bag is placed in the trough of the structured packing. This kind of catalyst packing member can not only realize the use of small particle catalyst, but also make the bed of the catalytic distillation reaction section have a larger porosity, and make the catalyst evenly distributed in the whole bed, and at the same time, the strength requirement of the catalyst is not high , but the catalyst loading is small.

Chinese patent CN200810052268.4 proposes a catalyst net box. Catalyst particles are arranged in a closed net box made of wire mesh and flat bridge with an anti-overflow baffle. Inside, catalyst mesh boxes of adjacent layers do not overlap on the same axis. It is characterized in that the catalyst is reasonably and effectively distributed in the tower, and with the anti-overflow baffle above the catalyst net box, the gravity potential energy of the liquid itself is used to make the liquid flow through the catalyst bed evenly from top to bottom, avoiding the leakage caused by the liquid The problem of slow renewal of the catalyst surface due to lateral diffusion to the catalyst surface; and there is a certain distance between the catalyst mesh boxes, that is, a large number of gas phase channels are set up, and mass transfer elements are placed in the gas phase channels, but the catalyst bed resistance is large and the catalytic Disadvantages of the small processing capacity of the rectification tower.

Utility model content

The purpose of the utility model is to provide a catalyst packing member in a catalytic rectification tower, which is suitable for a catalytic rectification tower for producing methyl tert-butyl ether by etherification of light gasoline. By adopting the catalyst packing member described in the utility model, the conversion rate of tertiary olefins in light gasoline can be improved, effective separation of methyl tert-butyl ether can be realized, and energy consumption can be effectively reduced.

The catalyst loading member described in the utility model is placed in a catalytic rectification tower, including a cylinder body and at least two trays arranged in the cylinder body, a number of tray holes are arranged on the trays, adjacent trays and cylinder body It constitutes a repeating unit, and there are several ventilation pipes vertically in the repeating unit. The top of the ventilation pipe is set under one tray, and the bottom is connected to another tray. In the repeating unit, ceramic rings and catalysts are sequentially added to form ceramic rings. layer and a catalyst layer, the height of the catalyst layer is lower than that of the ventilation pipe, the top of the ventilation pipe is connected with a ventilation pipe cap, and the top of the ventilation pipe is provided with a number of ventilation holes along the joint with the ventilation pipe cap.

The top of the ventilation pipe is zigzag or wavy.

The number of vent holes is 4-10, through which the gas escapes during the reaction process, which can effectively increase the mass transfer efficiency.

The ventilation pipe cap is umbrella-shaped, the diameter of the ventilation pipe cap is larger than the diameter of the ventilation pipe, and the ventilation pipe cap is provided with cap holes around the periphery of the ventilation pipe.

The opening rate on the vent pipe cap is 10%-80%.

The opening rate on the vent pipe cap is 40%-60%.

The side wall of the ventilation pipe is provided with a through hole, which is beneficial for the gas generated by the reaction to escape through the through hole, thereby increasing the mass transfer between the gas and liquid phases.

The diameter of the ventilation pipe is 0.05-0.2 of the diameter of the tray.

1 to 12 vent pipes are arranged on each tray.

4 to 8 vent pipes are arranged on each tray.

The advantage of the catalytic rectification filling member described in the utility model is:

1. In the catalyst packing member described in the utility model, due to the distribution of several ventilation pipes, the upwardly flowing gas can pass through the catalyst bed along the gas phase channel, pass through the ventilation hole at the top of the ventilation pipe smoothly, and then meet with the liquid phase above the catalyst packing layer. Contact: Since there are through holes on the side wall of the ventilation pipe, part of the gas phase can directly contact the liquid phase in the catalyst layer through the through holes, and the combined action of the two can effectively carry out gas-liquid mass transfer. On the one hand, it avoids the wear and tear of the catalyst caused by the upward flow of gas; Reduce energy consumption.

2. In the catalyst loading component of the present utility model, vent pipes vertical to it are distributed on the tray, and the gas phase channel of the vent pipe divides the same loading component into a liquid-solid reaction zone and a gas-liquid reaction zone, and the liquid flowing down in the upper tray depends on itself Gravity, through the tray hole on the tray, and the bottom-up gas mass transfer can evenly pass through the catalyst bed. The residence time of the liquid on the catalyst is increased, the reaction is promoted, and the conversion rate of tertiary olefins in light gasoline can be increased.

3. In the catalyst loading component of the present utility model, cap holes are distributed on the cap of the ventilation pipe to allow the liquid flowing down from the upper tray to pass through evenly. The cap holes can effectively disperse the liquid, promote the reaction, and increase the amount of tertiary carbon in light gasoline. Olefin conversion.

Description of drawings:

The sectional structure schematic diagram of Fig. 1 utility model repeating unit;

Fig. 2 is the top view structure schematic diagram of the utility model tray;

Fig. 3 is the top view structure schematic diagram of the catalyst packing member of the utility model;

Fig. 4 is a schematic cross-sectional structure diagram of the utility model ventilation pipe;

Fig. 5 is a schematic diagram of the cross-sectional structure of the filling member of the utility model;

In the figure, 1. Cylinder body, 2. Tray, 3. Porcelain ring layer, 4. Catalyst layer, 5. Vent pipe, 6. Vent hole, 7. Vent pipe cap, 8. Cap hole, 9. Vent Holes, 10. Tray wells, 11. Repeating units.

Detailed ways

The utility model is further described in detail by the following examples, but these examples should not be considered as a limitation of the utility model.

Below in conjunction with accompanying drawing, the utility model is described in further detail.

Example 1

Referring to Figures 1 to 5, a catalyst packing member is placed in a catalytic rectification tower, including a cylinder 1 and at least two trays 2 arranged in the cylinder 1, and adjacent trays 2 and cylinder 1 constitutes a repeating unit 11, in which a number of ventilation pipes 5 are longitudinally arranged, and the top of the ventilation pipe 5 is arranged below a tray 2, and the bottom thereof is connected with another tray 2, and is sequentially added in the repeating unit 11 Porcelain ring and catalyst form ceramic ring layer 3 and catalyst layer 4 respectively, and the height of catalyst layer 4 is lower than the height of vent pipe 5, and the top of vent pipe 5 is connected with vent cap 7, and the top of vent pipe 5 is along with vent pipe. The junction of the trachea cap 7 has a number of air holes 6, the number of air holes 6 is 4, 6, 8 or 10, the top of the air pipe 5 is zigzag or wavy, and the side wall of the air pipe 5 Have through hole 9.

The tray 2 is provided with a plurality of tray holes 10 through which the gas phase in the tower can pass. The tray 2 can be made of 20-150 mesh stainless steel wire mesh, perforated steel plate with a porosity of 10%-80%, porous ceramics or porous silicon carbide.

The vent pipe cap is umbrella-shaped, the diameter of the vent pipe cap 7 is greater than the diameter of the vent pipe 5, and the vent pipe cap 7 has a cap hole 8 around the vent pipe 5, and the vent pipe cap 7 The opening ratio on the top is 10%, 40%, 60% or 80%. The diameter of the ventilation pipe 5 is 0.05 to 0.2 of the diameter of the tray 2. One, four, or 6, 8 or 12.

The ventilation pipe cap 7 is umbrella-shaped, and the part beyond the diameter of the ventilation pipe is a circular horizontal outer eaves with an opening rate of 10% to 80%; the top of the ventilation pipe cap is closed to effectively prevent the upper catalyst from falling into the ventilation pipe The part beyond the diameter of the ventilation pipe is a circular horizontal eaves with openings, which can evenly and effectively distribute the liquid flowing down from the upper layer and improve the mass transfer efficiency.

The internal diameter of the catalytic rectification tower is 60mm, the structured packing of the rectifying section of the tower is filled with 300mm, the stripping section of the tower is filled with the structured packing of 1000mm, and the structured packing is Ring, the reactor is filled with a macroporous styrene-based strong acid cation resin as an etherification catalyst and a ceramic ring with a diameter of 2mm and a height of 4mm. The various parameters of the catalyst packing components used are shown in Table 1.

Table 1

The raw material of light gasoline enters the feed port of the catalytic rectification tower from the feed port of the rectification tower to carry out the catalytic rectification reaction of catalytic light gasoline etherification. The inlet temperature is 60°C and the operating pressure is 0.2MPaG. The conversion rate of C5 tertiary olefins was 84.18%, the conversion rate of C6 tertiary olefins was 53.90%, the conversion rate of total tertiary olefins was 73.48%, and the content of total ether compounds in the bottom product of the catalytic rectification tower was 48.02w%.

In the catalyst loading component of the utility model, the gas phase channel of the ventilation pipe divides the repeating unit into a liquid-solid reaction zone and a gas-liquid reaction zone. After mass transfer, the gas on the top can evenly pass through the catalyst bed, which can effectively avoid the wear and tear of the catalyst caused by the upward flow of gas, reduce the pressure drop of the bed, enhance the gas-liquid mass transfer capacity, and effectively distribute the liquid , promote the reaction, and increase the conversion rate of tertiary olefins in light gasoline. During the etherification reaction process, the catalyst packing member can realize effective separation of methyl tert-butyl ether, and can effectively reduce energy consumption.

Of course, the utility model can also have other various embodiments, and those skilled in the art can make various corresponding changes and deformations according to the utility model without departing from the spirit and essence of the utility model. But these corresponding changes and deformations should all belong to the scope of protection of the appended claims of the present utility model.

Claims (10)

1. a Catalyst packing component, be placed in catalytic rectifying tower, it is characterized in that, comprise cylindrical shell and be arranged at least two column plates in cylindrical shell, described column plate is provided with some column plate holes, adjacent tray and cylindrical shell form repetitive, longitudinally some breather pipes are provided with in described repetitive, the top of described breather pipe is arranged on the below of a column plate, be connected with another column plate bottom it, porcelain ring is added successively and catalyst forms porcelain circular layer and catalyst layer respectively in repetitive, the height of described catalyst layer is lower than the height of breather pipe, the top of described breather pipe is connected with breather pipe calotte, and breather pipe top has some passages along the junction with breather pipe calotte.

2. Catalyst packing component according to claim 1, is characterized in that, the top of described breather pipe is zigzag or waveform.

3. Catalyst packing component according to claim 1 and 2, is characterized in that, described passage number is 4 ~ 10.

4. Catalyst packing component according to claim 1, is characterized in that, described breather pipe calotte is umbrella shape, and the diameter of described breather pipe calotte is greater than the diameter of breather pipe, and the surrounding that breather pipe calotte exceeds breather pipe has calotte hole.

5. Catalyst packing component according to claim 4, is characterized in that, the percent opening on described breather pipe calotte is 10% ~ 80%.

6. Catalyst packing component according to claim 5, is characterized in that, the percent opening on described breather pipe calotte is 40% ~ 60%.

7. Catalyst packing component according to claim 1, is characterized in that, the sidewall of described breather pipe has through hole.

8. Catalyst packing component according to claim 1, is characterized in that, described breather pipe diameter is 0.05 ~ 0.2 of tray diameter.

9. Catalyst packing component according to claim 1, is characterized in that, described breather pipe is arranged 1 ~ 12 on every layer of column plate.

10. Catalyst packing component according to claim 9, is characterized in that, described breather pipe is arranged 4 ~ 8 on every layer of column plate.