CN214106875U - Trickle bed reactor - Google Patents

Trickle bed reactor Download PDF

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Publication number
CN214106875U
CN214106875U CN202022033839.9U CN202022033839U CN214106875U CN 214106875 U CN214106875 U CN 214106875U CN 202022033839 U CN202022033839 U CN 202022033839U CN 214106875 U CN214106875 U CN 214106875U
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bed reactor
trickle bed
liquid
gas
distributor
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李木金
杨卫胜
施德
黄云群
赵鹏
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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Abstract

The utility model discloses a trickle bed reactor, which comprises a shell, a feed inlet and a discharge outlet on the surface of the shell, and a gas-liquid distributor inside the shell, wherein the gas-liquid distributor comprises a distribution plate and a distribution pipe; the distribution pipe comprises a top cover, a vertical short pipe and a conical flow crusher; a gap is formed between the top cover and the upper end of the vertical short pipe; the vertical short pipe penetrates through the distribution plate, and a small hole is formed in the side wall of the vertical short pipe; the surface of the conical flow crusher is provided with round holes and/or slits, and optionally, a gap is formed between the bottom end of the vertical short pipe and the conical flow crusher. The trickle bed reactor of the utility model has the characteristic of even gas-liquid distribution, and especially has good distribution effect when processing the fluid with large liquid phase load change.

Description

Trickle bed reactor
Technical Field
The utility model relates to a trickle bed reactor.
Background
The trickle bed reactor is a gas-liquid-solid three-phase catalytic reactor, and gas and liquid flow through a solid catalyst bed layer in parallel, so that the trickle bed reactor is widely applied to chemical fields of petroleum refining (hydrocracking, hydrofining, hydroisomerization, hydrodearomatization and the like), petrochemical industry (hydrogenation, hydration, oxidation and the like), fine chemical industry, environmental engineering and the like. Trickle-bed reactors have incomparable advantages in large-scale processing, high-pressure operation of heterogeneous catalytic processes. However, the gas-liquid cocurrent mode easily causes uneven liquid flow, causes partial catalyst not to be well wetted, affects reaction effect, and more possibly causes temperature runaway of the reactor for strong exothermic reaction. Thus, whether the liquid is uniformly distributed in the reactor directly affects the uniformity of the contact time of the reactants with the catalyst, and the degree to which the surface of the catalyst is wetted by the liquid phase. The uneven gas-liquid distribution can form phenomena of bias flow, local short circuit and the like, and finally influences the exertion of the function of the catalyst and the quality of reaction products, so the importance of gas-liquid medium distribution is more prominent.
Trickle-bed reactors typically employ a gas-liquid distributor to distribute the gas-liquid medium uniformly over the underlying catalyst bed. The existing gas-liquid distributors are generally divided into three types of long and short pipes: overflow, suction, and a combination thereof.
CN101279228B discloses a gas-liquid distributor of trickle bed reactor, which mainly has small holes around the liquid phase short tube, to solve the problem that the liquid and gas only have axial flow distribution and are difficult to form uniform gas-liquid distribution, but the distributor still has the disadvantage that when the liquid flows out of the main tube, the liquid drops are large, even the center confluence phenomenon occurs.
CN2355786Y discloses a gas-liquid distributor, which is provided with a crushing plate with symmetrically distributed slits at the bottom edge of the central tube of the traditional suction gas-liquid distributor, so as to increase the spraying area of the liquid to a certain extent, improve the distribution effect of the gas-liquid (especially high viscosity medium), but still have a central flow which is not easy to disperse in the lower area of the center of the crushing plate; when the liquid phase load is great, the distribution effect is not good, and the distributor has a complex structure and is troublesome to install and maintain.
CN205127915U discloses a trickle bed reactor, wherein a gas channel and a liquid channel are arranged on a gas-liquid distributor, the advantages of simple structure, dense arrangement and the like of the original overflow type gas-liquid distributor are reserved, liquid phase small holes are arranged on the side surface of the liquid channel, meanwhile, a flow crushing plate is additionally arranged at the tail end of the liquid channel, but the gas phase and the liquid phase of the trickle bed reactor cannot be premixed; liquid pores on the distributor are at the lowest point of the distributor, and when easily scaled impurities or particle impurities exist in the feed, the impurities are easily deposited to block the pores, so that the distribution is uneven; when the load change of the treated liquid phase is large, the distributor cannot give consideration to two working conditions of large flow and small flow, and the problem of uneven distribution still easily occurs; and because the liquid is distributed independently, the flow velocity is too fast and too concentrated, and the liquid can not be dispersed effectively, so that the effect of subsequent reaction is influenced.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that prior art has the gas-liquid uneven distribution, especially under handling different work condition (like catalyst initial stage, last stage operating mode), the great technology of liquid phase load change in the reactor, and the relatively poor problem of distribution effect provides a new trickle bed reactor. The trickle bed reactor has the characteristic of uniform gas-liquid distribution, and particularly has good distribution effect and large operation elasticity when treating fluid with large liquid phase load change.
In the present invention, unless otherwise specified, the terms of orientation such as "upper, lower, left, right, top, side" used herein generally refer to the upper, lower, left, right, top, side shown in the drawings; "inner and outer" refer to the inner and outer relative to the profile of the components themselves.
The utility model provides a trickle bed reactor, which comprises a shell, a feed inlet and a discharge outlet on the surface of the shell, and a gas-liquid distributor inside the shell, wherein,
the gas-liquid distributor comprises a distribution plate and a distribution pipe;
the distribution pipe comprises a top cover, a vertical short pipe and a conical flow crusher; a gap is formed between the top cover and the upper end of the vertical short pipe; the vertical short pipe penetrates through the distribution plate, and a small hole is formed in the side wall of the vertical short pipe; the surface of the conical flow crusher is provided with round holes and/or slits,
optionally, the bottom end of the vertical stub forms a gap with the conical shaped flow crusher.
According to some embodiments of the present invention, the distribution pipe is a plurality of distribution pipes, and a schematic diagram of one distribution pipe can be shown in fig. 2 a.
According to some embodiments of the invention, the conical flow crusher has a bottom angle α of 20 ° to 170 °. The included bottom angle alpha may be as shown in fig. 2 a.
According to some embodiments of the invention, the bottom of toper current breaker sets up the round hole.
According to some embodiments of the invention, the tapered flow crusher is circumferentially provided with a strip slit. In the present invention, the shape of the slit has no special requirements, such as the long slit shown in fig. 2 d.
According to some embodiments of the present invention, the diameter D1 of the bottom end circular hole of the cone-shaped flow crusher may be determined according to working conditions, such as but not limited to: d1 is 3mm-10 mm.
According to some embodiments of the invention, the ratio of the total area S1 of the circular holes and/or slits provided in the surface of the conical flow breaker to the cross-sectional area S2 of the standing stub is 0.5:1 to 1: 1. In the present invention, the "cross-sectional area of the vertical stub pipe" refers to a sectional area of the pipe of the vertical stub pipe.
According to some embodiments of the invention, the ratio of the height h2 of the gap between the bottom end of the vertical stub and the conical flow crusher to the vertical stub inner diameter D3 is 0:4-1:4, preferably 0.1:4-1: 4. The height h2 may be as shown in fig. 2a as h 2.
According to some embodiments of the invention, the top side wall of the vertical stub is provided with an overflow groove. Further preferably, two overflow grooves which are opposite to each other at 180 degrees are arranged on the side wall of the top end of the vertical short pipe. As shown in fig. 2 b.
According to some embodiments of the invention, the ratio of the total area S3 of the overflow groove to the cross-sectional area S2 of the standing stub is 1:5 to 1: 20.
According to some embodiments of the present invention, the side wall of the vertical stub is provided with one or more layers of small holes; preferably two or more layers.
According to some embodiments of the present invention, the diameter D2 of each small hole may be determined according to the working conditions, such as but not limited to: d2 is 3mm-10 mm.
According to some embodiments of the utility model, the high interval of upper and lower two-layer aperture can be decided according to the operating mode, for example but not limited to: the height interval between the upper layer of small holes and the lower layer of small holes is 20mm-60 mm.
According to some embodiments of the present invention, each layer is provided with two mutually 180 ° facing apertures. For example, as shown in fig. 2c, the apertures of each layer are oriented 180 ° relative to each other.
According to some embodiments of the invention, the pores of each layer preferably have the same pore size.
According to some embodiments of the present invention, the ratio of the diameters of the upper and lower layers of pores is 1:1-0.3: 1. Under the optimal conditions, the diameter of the small holes is reduced from bottom to top or has the tendency of reduction (for example, the diameter is reduced firstly and then is the same), which is beneficial to improving the liquid level height above the upper layer of small holes, improving the uniformity of the overall distribution in the reactor and improving the operation elasticity.
According to some embodiments of the invention, the open area ratio of the vertical stub pipes on the distribution plate is 5% to 20%.
According to some embodiments of the invention, the top cover is a flat top cover (top cover in the form of a flat plate). It is further preferred that the height h1 of the gap between the top cap and the upper end of the standing nipple is in a ratio of 0.25:1 to 1:1 to the standing nipple inner diameter D3. Lowering the height of h1 reduces the probability of liquid entering the vertical stub directly without passing through the distribution apertures, improving the uniformity of liquid distribution, but too low an h1 increases the pressure drop in the gas phase. The height h1 may be as shown in fig. 2 a.
According to some embodiments of the invention, the ratio of the diameter D4 of the top cover to the inner diameter D3 of the standing nipple is 1:1-2: 1.
According to some embodiments of the invention, the feed inlet comprises a gas feed inlet and a liquid feed inlet.
According to some embodiments of the invention, the trickle bed reactor further comprises a gas pre-distributor in communication with the gas feed inlet.
According to some embodiments of the invention, the gas predistributor is arranged at the top of the reactor housing.
According to some embodiments of the invention, the trickle bed reactor further comprises a liquid pre-distributor in communication with the liquid feed inlet.
According to some embodiments of the utility model, the liquid is divided into two parts, namely the gas distributor and the liquid distributor.
According to some embodiments of the present invention, the liquid predistributor comprises a main feeding pipe, a distribution branch pipe, a downcomer and a baffle; the distribution branch pipes are communicated with the feeding main pipe, the downcomer vertically penetrates through the distribution branch pipes, and the bottom of the downcomer is provided with a baffle.
According to some embodiments of the present invention, the ratio of the total area of the feeding main pipe S4 to the total area of the downcomer S5 is 0.6:1 to 1: 1.
According to some embodiments of the invention, the discharge port comprises a gas phase product outlet and a liquid phase product outlet.
According to some embodiments of the invention, the gas phase product outlet is provided in a lower middle side wall of the reactor shell.
According to some embodiments of the invention, the liquid product outlet is provided at the bottom end of the reactor housing.
In the utility model, gas phase materials enter the reactor through the gas feed inlet, liquid phase materials enter the reactor through the liquid feed inlet, the gas phase materials reach the gas-liquid distributor after being uniformly distributed by the gas pre-distributor and enter the vertical short pipe through the gap between the flat top cover and the upper end of the vertical short pipe and the small hole on the vertical short pipe, and the flat top cover prevents the liquid phase from directly entering the vertical short pipe through the gap; liquid phase materials enter a feeding main pipe of the liquid pre-distributor, enter a gas-liquid distributor through a distribution branch pipe, a downcomer and a baffle at the bottom of the downcomer, and then are accumulated on the gas-liquid distributor to form a liquid phase, when the height of the liquid phase is higher than that of the small hole on the side wall of the vertical short pipe, the liquid phase enters the vertical short pipe from the small hole, and when the liquid phase load is larger, the height of the liquid phase reaches the height of an overflow groove on the side wall of the top end of the vertical short pipe and enters the vertical short pipe from the overflow groove; the gas-phase material and the liquid-phase material interact in the vertical short pipe and are uniformly mixed; gas-liquid phase materials flow downwards to the conical flow crusher at the bottom through the vertical short pipe, gas-liquid phase materials flow to the ceramic ball layer through the round hole at the bottom end of the conical flow crusher and preferably through the strip seam arranged along the circumference of the conical flow crusher and the gap between the bottom end of the vertical short pipe and the conical flow crusher; the gas-liquid phase material enters a catalyst bed layer after passing through a ceramic ball layer, a gas-liquid phase reactor product is obtained after the reaction of the catalyst bed layer, and the product reaches the bottom space of the reactor through a bottom ceramic ball layer; and gas-liquid separation is directly carried out in the bottom space, gas phase is discharged from a gas phase product outlet on the side surface to obtain a gas phase product, and liquid phase is discharged from a liquid phase product outlet on the bottom to obtain a liquid phase product.
The utility model discloses a set up the garrulous stream ware into the toper, and this toper garrulous stream ware surface sets up round hole and/or strip seam, the bottom and the toper garrulous stream ware of the preferred vertical nozzle stub are formed with the space for gaseous and gaseous area of spraying from the vertical nozzle stub outflow receives gas, the undulant influence of liquid phase load diminishes, when handling the great fluid of liquid phase load, also can be better respectively the fluid, the liquid velocity of flow is too fast, too concentrated phenomenon can not appear, thereby be favorable to subsequent catalytic reaction at the catalyst bed.
Furthermore, the utility model discloses in the preferred embodiment, make the relatively even income gas-liquid distributor of liquid phase reaction material through setting up liquid predistributor for liquid level on the gas-liquid distribution dish is relatively even, improves the overall distribution effect of liquid on the gas-liquid distribution dish.
Furthermore, the utility model discloses in the preferred embodiment, set up multilayer aperture, top lateral wall at the side of the nozzle stub of standing vertically and set up the overflow recess, especially the aperture diameter reduces or has the trend of reducing from bottom to top according to a certain proportion, is favorable to improving the liquid level height more than the upper aperture, improves the homogeneity of the total distribution in the reactor, has improved the operation elasticity of liquid phase load.
Drawings
Fig. 1 is a general schematic diagram of a trickle bed reactor provided in example 1 of the present invention.
Fig. 2a is a schematic structural diagram of a distribution pipe of a trickle bed reactor provided in example 1 of the present invention;
FIG. 2b is a view in the direction M of FIG. 2 a;
FIG. 2c is a top view of section A-A of FIG. 2 a;
FIG. 2d is a sectional top view B-B of FIG. 2 a;
fig. 3a is a schematic top view of a liquid pre-distributor of a trickle bed reactor according to example 1 of the present invention;
fig. 3b is a cross-sectional view a-a of fig. 3 a.
Description of the reference numerals
1. Casing 2, gas-liquid distributor 21, distributing plate
221. Top cover 222, upright stub 2221, overflow groove
2222. Small hole 223, conical flow crusher 2231, round hole
2232. Strip seam 3, gas feed inlet 4 and liquid feed inlet
5. Gas pre-distributor 6, liquid pre-distributor 61 and feeding main pipe
62. Distribution branch 63, downcomer 64, baffle
7. Gas phase product outlet 8, liquid phase product outlet 9 and ceramic ball layer
10. Catalyst bed layer 11, bottom ceramic ball layer
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention easier to understand, the present invention will be further described in detail with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention.
[ example 1 ]
A trickle-bed reactor, as shown in FIG. 1, FIG. 2a to FIG. 2d, FIG. 3a and FIG. 3b, comprises a shell 1, a gas feed port 3, a liquid feed port 4, a gas phase product outlet 7 and a liquid phase product outlet 8 which are sequentially arranged from top to bottom on the surface of the shell 1, and a gas pre-distributor 5 communicated with the gas feed port 3, a liquid pre-distributor 6 communicated with the liquid feed port 4 and a gas-liquid distributor 2 which are sequentially arranged from top to bottom inside the shell.
Wherein, the gas-liquid distributor 2 comprises a distribution plate 21 and a distribution pipe; the distribution pipe comprises a flat top cover 221, an upright short pipe 222 and a conical flow crusher 223; a gap is formed between the flat top cover 221 and the upper end of the vertical short pipe 222; the vertical short pipe 222 penetrates through the distribution plate 21, and a small hole 2222 is formed in the side wall of the vertical short pipe 222; the surface of the conical flow crusher 223 is provided with round holes and slits, and the bottom end of the vertical short pipe 222 forms a gap with the conical flow crusher 223.
Wherein, the liquid pre-distributor 6 comprises a main feeding pipe 61, a distribution branch pipe 62, a downcomer 63 and a baffle 64; the distribution branch pipe 62 is communicated with the feeding main pipe 61, the downcomer 63 vertically penetrates through the distribution branch pipe 62, and the bottom of the downcomer 63 is provided with a baffle plate 64.
Wherein the diameter of the trickle bed reactor is 2000mm, and the ratio of the total area S4 of the feeding main pipe of the liquid pre-distributor to the total area S5 of the downcomer is 1: 1.
The ratio of the height h1 of the gap between the flat top cover 221 on the gas-liquid distributor 2 and the upper end of the vertical short pipe 222 to the inner diameter D3 of the vertical short pipe is 0.4: 1; the ratio of the diameter D4 of the flat top cover to the inner diameter D3 of the vertical short pipe is 1.5: 1; the vertical stub 222 has an aperture ratio of 5% in the distribution plate 21.
The small holes 2222 on the vertical short pipe 222 are arranged in three layers at different heights, and two small holes which are opposite to each other at 180 ℃ are arranged at each layer of height. The diameters D2 of the three layers of small holes are respectively 8mm, 6 mm and 4mm from bottom to top, and the height interval between the upper layer of small holes and the lower layer of small holes is 40 mm.
The bottom end of the conical flow crusher 223 is provided with a circular hole 2231, and the conical flow crusher is provided with 8 slots 2232 along the circumference. The diameter D1 of the circular hole 2231 at the bottom of the conical shaped flow reducer 223 is 4mm, and the ratio of the total area S1 of the circular hole 2231 and the slits 2232 provided on the surface of the conical shaped flow reducer to the cross-sectional area S2 of the upright stub 222 is 0.8: 1. The included angle alpha of the bottom end of the conical flow crusher is 120 degrees. The height h2 of the gap between the bottom end of the vertical stub and the tapered flow reducer is 0.2:4 to the vertical stub inner diameter D3.
Two overflow grooves 2221 which are opposite to each other at 180 degrees are arranged on the side wall of the top end of the vertical short pipe 222, and the ratio of the total area S3 of the overflow grooves 2221 to the cross-sectional area S2 of the vertical short pipe 222 is 1: 10.
In this embodiment, gas-phase materials and liquid-phase materials enter the reactor through the gas feed inlet 3 and the liquid feed inlet 4, the gas-phase materials are uniformly distributed by the gas pre-distributor 5 and then reach the gas-liquid distributor 2, and enter the vertical short pipe through the gap between the flat top cover 221 and the upper end of the vertical short pipe 222 and the small holes 2222 on the vertical short pipe 222, and the flat top cover 221 prevents the liquid phase from directly entering the vertical short pipe 222 through the gap; the liquid phase material enters a main feeding pipe 61 of the liquid pre-distributor 6, enters the gas-liquid distributor 2 through a distribution branch pipe 62, a downcomer 63 and a baffle plate 64 at the bottom of the downcomer, then is accumulated on the gas-liquid distributor 2 to form a liquid phase, when the height of the liquid phase is higher than that of the small holes on the side walls of the vertical short pipes, the liquid phase enters the vertical short pipes 222 from the small holes 2222, and when the load of the liquid phase is larger, the height of the liquid phase reaches the height of overflow grooves 2221 on the side walls at the top ends of the vertical short pipes and enters the vertical short pipes 222 from the overflow grooves 2221; the gas-phase material and the liquid-phase material interact in the vertical short pipe 222 and are uniformly mixed; the gas-liquid phase material flows downwards to the conical flow crusher 223 at the bottom through the vertical short pipe 222, and the gas-liquid phase material is sprayed to the ceramic ball layer through a round hole 2231 at the bottom end of the conical flow crusher, a strip slit 2232 arranged along the circumference of the conical flow crusher and a gap between the bottom end of the vertical short pipe and the conical flow crusher; the gas-liquid phase material enters a catalyst bed layer 10 after passing through a ceramic ball layer 9, a gas-liquid phase reactor product is obtained after the reaction of the catalyst bed layer 10, and the product reaches the bottom space of the reactor through a bottom ceramic ball layer 11; and gas-liquid separation is directly carried out in the bottom space, gas phase is discharged from a side gas phase product outlet 7 to obtain a gas phase product, and liquid phase is discharged from a bottom liquid phase product outlet 8 to obtain a liquid phase product.
[ example 2 ]
The trickle bed reactor comprises a shell, a gas feed inlet, a liquid feed inlet, a gas-phase product outlet and a liquid-phase product outlet which are sequentially arranged on the surface of the shell from top to bottom, and a gas pre-distributor, a liquid pre-distributor and a gas-liquid distributor which are sequentially arranged inside the shell from top to bottom and are communicated with the gas feed inlet.
Wherein, the gas-liquid distributor comprises a distribution plate and a distribution pipe; the distribution pipe comprises a flat top cover, a vertical short pipe and a conical flow crusher; a gap is formed between the flat top cover and the upper end of the vertical short pipe; the vertical short pipe penetrates through the distribution plate, and the side wall of the vertical short pipe is provided with a small hole; the surface of the conical flow crusher is provided with round holes and strip slits.
The liquid pre-distributor comprises a feeding main pipe, distribution branch pipes, a downcomer and a baffle; the distribution branch pipe is communicated with the feeding main pipe, the downcomer vertically penetrates through the distribution branch pipe, and the bottom of the downcomer is provided with a baffle.
Wherein the diameter of the trickle bed reactor is 3000mm, and the ratio of the total area S4 of the feeding main pipe of the liquid pre-distributor to the total area S5 of the downcomer is 0.6: 1.
The ratio of the height h1 of a gap between the flat top cover on the gas-liquid distributor and the upper end of the vertical short pipe to the inner diameter D3 of the vertical short pipe is 1: 1; the ratio of the diameter D4 of the flat top cover to the inner diameter D3 of the vertical short pipe is 1: 1; the open area of the vertical short pipe on the distribution plate is 20%.
The small holes on the vertical short pipe are provided with three layers at different heights, and each layer is provided with two small holes which are opposite to each other at 180 ℃. The diameters of the three layers of small holes are respectively 4mm, 3mm and 3mm from bottom to top, and the height interval between the upper layer of small holes and the lower layer of small holes is 60 mm.
The bottom of toper breaker sets up the round hole, and toper breaker sets up 10 strip seams along the circumference. The diameter D1 of the round hole at the bottom of the conical flow reducer is 8mm, and the ratio of the total area S1 of the round hole and the strip slot arranged on the surface of the conical flow reducer to the cross-sectional area S2 of the vertical short pipe is 0.5: 1. The included angle alpha of the bottom end of the conical flow crusher is 160 degrees. The ratio of the height h2 of the gap between the bottom end of the vertical stub and the tapered flow reducer to the vertical stub inner diameter D3 is 0: 4.
Two overflow grooves which are opposite to each other at an angle of 180 degrees are arranged on the side wall of the top end of the vertical short pipe, and the ratio of the total area S3 of the overflow grooves to the cross-sectional area S2 of the vertical short pipe is 1: 5.
In the embodiment, gas-phase materials and liquid-phase materials enter the reactor through the gas feed inlet and the liquid feed inlet, the gas-phase materials are uniformly distributed by the gas pre-distributor and then reach the gas-liquid distributor, and enter the vertical short pipe through a gap between the flat top cover and the upper end of the vertical short pipe and the small holes on the vertical short pipe, and the flat top cover prevents the liquid phase from directly entering the vertical short pipe through the gap; liquid phase materials enter a feeding main pipe of the liquid pre-distributor, enter a gas-liquid distributor through a distribution branch pipe, a downcomer and a baffle at the bottom of the downcomer, and then are accumulated on the gas-liquid distributor to form a liquid phase, when the liquid phase is higher than small holes in the side wall of the vertical short pipe, the liquid phase enters the vertical short pipe from the small holes, and when the liquid phase load is large, the liquid phase reaches the height of an overflow groove in the side wall of the top end of the vertical short pipe and enters the vertical short pipe from the overflow groove; the gas-phase material and the liquid-phase material interact in the vertical short pipe and are uniformly mixed; gas-liquid phase materials flow downwards to the conical flow crusher at the bottom through the vertical short pipe, and gas-liquid phase materials are sprayed to the ceramic ball layer through the circular hole at the bottom end of the conical flow crusher and the strip seam arranged along the circumference of the conical flow crusher; the gas-liquid phase material enters a catalyst bed layer after passing through a ceramic ball layer, a gas-liquid phase reactor product is obtained after the reaction of the catalyst bed layer, and the product reaches the bottom space of the reactor through a bottom ceramic ball layer; and gas-liquid separation is directly carried out in the bottom space, gas phase is discharged from a gas phase product outlet on the side surface to obtain a gas phase product, and liquid phase is discharged from a liquid phase product outlet on the bottom to obtain a liquid phase product.
[ example 3 ]
Respectively introducing mixed liquid (3% by weight of nitric acid, 20% by weight of water and 77% by weight of methanol) containing nitric acid, water and methanol and mixed gas (70% by volume of nitrogen, 5% by volume of methyl nitrite, 10% by volume of carbon monoxide, 5% by volume of methanol and 10% by volume of NO) containing NO discharged from the tower bottom of the oxidative esterification tower into the trickle bed reactor in example 1 at a reaction temperature of 85 ℃, a reaction pressure of 0.5MPaG and a liquid hourly space velocity of 1h-1The molar ratio of NO to nitric acid was 5, and the conversion of nitric acid was 98.2% (calculated as 1-total nitric acid at the outlet of the reactor/total nitric acid at the inlet of the reactor x 100%).
[ example 4 ]
Respectively introducing mixed liquid containing nitric acid, water and methanol (the nitric acid content is 1.5 wt%, the water content is 10 wt%, and the methanol content is 88.5 wt%) and mixed gas containing NO (70 vol% of nitrogen, 5 vol% of methyl nitrite, 10 vol% of carbon monoxide, 5 vol% of methanol, and 10 vol% of NO) discharged from the tower bottom of the oxidative esterification tower into the trickle bed reactor in example 1 at a reaction temperature of 85 ℃, a reaction pressure of 0.5MPaG, and a liquid hourly space velocity of 2h-1The reaction was carried out at a molar ratio of NO to nitric acid of 5 to produce methyl nitrite, the conversion of nitric acid was 97.0%.
[ example 5 ]
Respectively introducing mixed liquid (nitric acid content 3 wt%, water content 20 wt%, methanol content 77 wt%) containing nitric acid, water and methanol and mixed gas (nitrogen gas 70 vol%, methyl nitrite 5 vol%, carbon monoxide 10 vol%, methanol 5 vol%, NO 10 vol%) containing NO discharged from the tower bottom of the oxidative esterification tower into the trickle bed reactor of example 2 at a reaction temperature of 85 ℃, a reaction pressure of 0.3MPaG and a liquid hourly space velocity of 1h-1The molar ratio of NO to nitric acid is 5 to generate methyl nitrite, and the conversion of nitric acidThe conversion rate was 97.5%.
Comparative example 1
The same raw materials and reaction conditions as those of example 3 of the present invention were used in accordance with the gas-liquid distributor of example 1 of CN 2015127915U. The nitric acid conversion was 97%.
Comparative example 2
The same raw materials and reaction conditions as those of example 4 of the present invention were used in accordance with the gas-liquid distributor of example 1 of CN 2015127915U. The nitric acid conversion was 93.5%.
Can find out through embodiment and comparative example, adopt the utility model discloses structural design's trickle bed reactor handles when the great technology of liquid phase load change, and the gas-liquid double-phase that gets into the catalyst bed distributes evenly, and the distribution effect is good, can gain fine reaction effect.
What has been described above is merely a preferred example of the present invention. It should be noted that other equivalent variations and modifications can be made by those skilled in the art based on the technical teaching provided by the present invention, and the protection scope of the present invention should be considered.

Claims (26)

1. A trickle bed reactor comprises a shell, a feed inlet and a discharge outlet on the surface of the shell, and a gas-liquid distributor in the shell, and is characterized in that,
the gas-liquid distributor comprises a distribution plate and a distribution pipe;
the distribution pipe comprises a top cover, a vertical short pipe and a conical flow crusher; a gap is formed between the top cover and the upper end of the vertical short pipe; the vertical short pipe penetrates through the distribution plate, and a small hole is formed in the side wall of the vertical short pipe; the surface of the conical flow crusher is provided with round holes and/or slits.
2. The trickle bed reactor of claim 1, wherein a gap is formed between a bottom end of the vertical stub and the tapered flow reducer.
3. The trickle bed reactor according to claim 1, wherein the included angle α of the bottom end of the conical shaped flow crusher is 20 ° to 170 °.
4. The trickle bed reactor according to claim 1, wherein the bottom end of the conical flow crusher is provided with a round hole and/or the conical flow crusher is provided with a slit along the circumference.
5. The trickle bed reactor according to claim 4, wherein the ratio of the total area S1 of the round holes and/or slits provided in the conical flow reducer surface to the cross-sectional area S2 of the standing stub is 0.5:1 to 1: 1.
6. The trickle bed reactor in accordance with claim 1, wherein the height h2 of the gap between the bottom end of the vertical stub and the tapered flow reducer is in a ratio of 0:4 to 1:4 to the vertical stub inner diameter D3.
7. The trickle bed reactor in accordance with claim 1, wherein the height h2 of the gap between the bottom end of the vertical stub and the tapered flow reducer is in a ratio of 0.1:4 to 1:4 to the vertical stub inner diameter D3.
8. The trickle bed reactor according to any one of claims 1-7, wherein the top end side wall of the upright stub is provided with an overflow recess.
9. The trickle bed reactor according to claim 8, wherein the top end side wall of the upright stub is provided with two overflow recesses facing 180 ° each other.
10. The trickle bed reactor according to claim 8, wherein the ratio of the total area S3 of the overflow recesses to the cross-sectional area S2 of the standing stub is 1:5 to 1: 20.
11. The trickle bed reactor according to any one of claims 1-7, wherein the side wall of the upstanding stub is provided with one or more layers of small holes.
12. The trickle bed reactor according to claim 11, wherein the side wall of the upstanding stub is provided with two or more layers of apertures.
13. The trickle bed reactor according to claim 11, wherein each layer is provided with two small holes facing each other at 180 °.
14. The trickle bed reactor of claim 11, wherein the ratio of the diameters of the upper and lower layers of apertures is from 0.3:1 to 1: 1.
15. The trickle bed reactor according to any one of claims 1 to 7, wherein the vertical stub has an open porosity of 5% to 20% in the distributor plate.
16. The trickle bed reactor according to any one of claims 1-7, wherein the top cover is a flat plate top cover.
17. The trickle bed reactor according to claim 6, wherein the height h1 of the gap between the top cover and the upper end of the vertical stub is 0.25:1 to 1:1 in ratio to the vertical stub inner diameter D3.
18. The trickle bed reactor in accordance with claim 16, wherein the ratio of the diameter D4 of the top cover to the inner diameter D3 of the vertical stub is 1:1 to 2: 1.
19. The trickle bed reactor according to any one of claims 1-7, wherein the feed ports include a gas feed port and a liquid feed port.
20. The trickle bed reactor in accordance with claim 19, further comprising a gas pre-distributor in communication with the gas feed inlet.
21. The trickle bed reactor of claim 20, wherein the gas pre-distributor is disposed at the top of the reactor housing.
22. The trickle bed reactor in accordance with claim 19, further comprising a liquid pre-distributor in communication with the liquid feed inlet.
23. The trickle bed reactor according to claim 22, wherein the liquid pre-distributor is disposed below the gas pre-distributor and above the gas-liquid distributor.
24. The trickle bed reactor according to claim 22, wherein the liquid pre-distributor includes a feed main, distribution legs, downcomers, and baffles; the distribution branch pipes are communicated with the feeding main pipe, the downcomer vertically penetrates through the distribution branch pipes, and the bottom of the downcomer is provided with a baffle.
25. The trickle bed reactor according to claim 24, wherein the ratio of the total area of the feed main tubes S4 to the total area of the downcomers S5 is from 0.6:1 to 1: 1.
26. The trickle bed reactor according to any one of claims 1-7, wherein the outlet port comprises a gas phase product outlet and a liquid phase product outlet.
CN202022033839.9U 2020-09-16 2020-09-16 Trickle bed reactor Active CN214106875U (en)

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