CN209952815U

CN209952815U - Vertical alkylation reaction device

Info

Publication number: CN209952815U
Application number: CN201920406114.4U
Authority: CN
Inventors: 黄旻; 胡先念
Original assignee: Yussen Chemical Co Ltd
Current assignee: Yussen Chemical Co Ltd
Priority date: 2019-03-27
Filing date: 2019-03-27
Publication date: 2020-01-17
Anticipated expiration: 2029-03-27

Abstract

The utility model discloses a vertical alkylation reaction device, which comprises a reactor, a first feeding pipe connected with a feeding port of the reactor, and two second feeding pipes which are distributed at two sides of the first feeding pipe in parallel and are equidistantly and connected with the feeding port of the reactor; the lower ends of the two second feeding pipes are respectively vertical and extend to be connected with the lower end of the first feeding pipe; the first-stage branch pipe is connected with the lower end of the first feeding pipe; a plurality of secondary branch pipes which are transversely and uniformly distributed around the primary branch pipe, wherein one end of each secondary branch pipe is connected with the primary branch pipe, and the other end of each secondary branch pipe is connected with the inner wall of the reactor; a plurality of three-stage branch pipes are uniformly connected below the two-stage branch pipes, and a plurality of through holes which are uniformly distributed are formed in the inner walls of the three-stage branch pipes. The reactor of the utility model has the advantages of simple structure, low cost, good mixing distribution effect and high space utilization rate.

Description

Vertical alkylation reaction device

Technical Field

The utility model relates to a chemical industry reaction instrument field especially relates to a vertical alkylation reaction device.

Background

Currently, environmental protection is a national policy in China and is always paid keen attention, automobile exhaust is one of the main factors causing air pollution, and the requirement on clean gasoline is higher and higher in order to advocate environmental protection. The alkylate oil has high octane number, low sulfur content, no olefin and no aromatic hydrocarbon, and is an ideal gasoline blending component.

In the chemical industry, the technologies adopted by the existing alkylation reaction mainly include sulfation method technology and hydrofluoric acid method technology. The alkylation reaction is that isobutane and butene react under the action of a strong acid catalyst to generate isooctane. The hydrofluoric acid method has great environmental hazard due to the high toxicity of hydrofluoric acid, and the process production cost of the hydrofluoric acid method is higher than that of the sulfuric acid method, so the hydrofluoric acid method is gradually eliminated. Currently, isooctane is prepared by adopting a sulfuric acid method. The traditional sulfuric acid alkylation reactors are divided into horizontal type and vertical type, and have different structural types. In the homogeneous phase distribution area, the liquid acid hydrocarbon is uniformly distributed and then enters the filler bed layer for alkylation reaction.

Chinese patent CN206391636U discloses a vertical coalescer, the inlet end of which is located outside the housing and is designed as a circular steel tube with a plurality of distributed holes on the tube wall to play the role of warm flow, an upper tube plate is arranged below the coalescer, a lower tube plate is arranged in the housing near the lower end enclosure, and a coalescing filter element located in the coalescing region is inversely arranged on the upper tube plate and extends downwards. However, when the device is used for alkylation reaction, the acid hydrocarbon cannot be fully covered on the cross section and uniformly mixed and distributed.

Chinese patent CN106693875A discloses a vertical alkylation reactor, the reactor part of which comprises a sulfuric acid distributor, a liquid hydrocarbon distributor and a gas phase C₄The catalyst sulfuric acid and the reaction hydrocarbon are respectively contacted and mixed with the liquid hydrocarbon distributor through the sulfuric acid distributor, and the reaction is carried out after the mixing and distribution. The device has longer distribution section, insufficient reaction and easy generation of more byproducts.

Chinese patent CN204799238U discloses a liquid-liquid fractal mixing device, which comprises a reactor, a fractal distributor a, a fractal distributor B, a distribution tray and a filler, wherein the fractal distributor a, the fractal distributor B, the distribution tray and the filler are sequentially arranged in the reactor from top to bottom. The fractal distributor A comprises a feeding pipe A, an annular pipe, a distribution pipe and a hose, and the fractal distributor B comprises a feeding pipe B, a primary distribution pipe and a secondary distribution pipe. The hose of the fractal distributor A and the secondary distribution pipe of the fractal distributor B are respectively connected with the feed inlet A and the feed inlet B on the distribution disc, the distribution disc is internally divided into an upper layer flow channel disc and a lower layer flow channel disc, each layer of flow channel is groove-type multi-stage H-shaped distribution, and outflow ports of the upper layer flow channel and the lower layer flow channel are correspondingly communicated. The device has a complex structure and a low space utilization rate.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to overcome prior art not enough and provide a vertical alkylation reaction device simple structure, mixed distribution are effectual, space utilization is high.

In order to achieve the above object, the utility model adopts the following technical scheme: the utility model provides a vertical alkylation reaction device, includes the reactor, connects the first inlet pipe and the parallel equidistant distribution of reactor feed inlet are in first inlet pipe both sides and with two second inlet pipes that the reactor feed inlet is connected still include: the lower ends of the two second feeding pipes are respectively vertical and extend to be connected with the lower end of the first feeding pipe; the first-stage branch pipe is connected with the lower end of the first feeding pipe; a plurality of secondary branch pipes which are transversely and uniformly distributed around the primary branch pipe, wherein one end of each secondary branch pipe is connected with the primary branch pipe, and the other end of each secondary branch pipe is connected with the inner wall of the reactor; a plurality of three-stage branch pipes are uniformly connected below the two-stage branch pipes, and a plurality of through holes which are uniformly distributed are formed in the inner walls of the three-stage branch pipes.

Furthermore, the three-level branch pipes are uniformly distributed below the two-level branch pipes in pairs, and each included angle between each three-level branch pipe and the horizontal plane is 45 degrees.

Furthermore, the tail end of the primary branch pipe and the tail end of the secondary branch pipe are both provided with pipe caps.

As a preferred embodiment of the present invention, the reactor diameter is 4.4m, the second feeding pipe diameter is 0.24m, the first feeding pipe diameter is 0.5m, the first-stage branch pipe diameter is 0.5m, the second-stage branch pipe diameter is 0.22m, and the third-stage branch pipe diameter is 0.07 m; the quantity of the second-stage branch pipes is 6, the quantity of the third-stage branch pipes is 36, and the quantity of the through holes formed in the third-stage branch pipes is 36.

Further, the diameter ratio of the second feeding pipe to the first feeding pipe is 0.5-0.6.

Furthermore, the diameter ratio of the distance between the two second feeding pipes and the reactor is 0.6-0.8.

Furthermore, the diameter ratio of the diameter of the secondary branch pipe to the diameter of the primary branch pipe is 0.4-0.6.

Furthermore, the diameter ratio of the diameter of the third-stage branch pipe to the diameter of the second-stage branch pipe is 0.3-0.5.

To sum up, the application the technical scheme of the utility model, following beneficial effect has: the reaction device of the utility model has the advantages of simple structure, good mixed distribution effect and high space utilization rate. The two liquids are respectively poured into the reactor from different independent pipelines and then collected in the same branch pipe, are fully mixed, are uniformly distributed, are divided into multi-stage multi-strand small-strand materials, are sprayed through the through holes, are uniformly covered on the space cross section of the whole reactor, and react. The reactor organically combines the material distribution area and the reaction area together, better saves space, improves the structure and simplifies the structure on the premise of ensuring the sufficient and uniform distribution of materials, and has the advantages of high mixing performance, simple structure, lower cost, good mixing and distribution effect, high space utilization rate and the like.

Drawings

FIG. 1 is a schematic structural view of a vertical alkylation reaction apparatus of the present invention;

FIG. 2 is a partial bottom view of the secondary branch and tertiary branch of the present invention;

fig. 3 is a longitudinal sectional view of the tertiary branch pipe of the present invention.

Reference is made to the accompanying drawings in which: 1-a second feeding pipe, 2-a reactor, 3-a first feeding pipe, 4-a first-stage branch pipe, 5-a second-stage branch pipe, 6-a third-stage branch pipe and 7-a through hole.

Detailed Description

The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, but the technical solution does not limit the scope of the present invention.

As shown in fig. 1 to 3, a vertical alkylation reaction apparatus mainly comprises: the device comprises a reactor 2, a first feeding pipe 3 connected with a feeding hole of the reactor 2, and two second feeding pipes 1 which are parallelly and equidistantly distributed on two sides of the first feeding pipe 3 and connected with the feeding hole of the reactor 2; the lower ends of the two second feeding pipes 1 are respectively vertical and extend to be connected with the lower end of the first feeding pipe 3; the first-stage branch pipe 4 is connected with the lower end of the first feeding pipe 3; a plurality of secondary branch pipes 5 are transversely and uniformly distributed around the primary branch pipe 4, one end of each secondary branch pipe 5 is connected with the primary branch pipe 4, the other end of each secondary branch pipe 5 is connected with the inner wall of the reactor 2, and pipe caps are arranged at the tail ends of the primary branch pipes 4 and the tail ends of the secondary branch pipes 5; a plurality of three-stage branch pipes 6 are uniformly connected below the two-stage branch pipes 5, and a plurality of through holes 7 which are uniformly distributed are formed in the inner walls of the three-stage branch pipes 6. The three-stage branch pipes 6 are uniformly distributed below the two-stage branch pipes 5 in pairs, and the included angle between each three-stage branch pipe 6 and the horizontal plane is 45 degrees.

Specifically, the diameter ratio of the second feeding pipe 1 to the first feeding pipe 3 is 0.5-0.6; the diameter ratio of the space between the two second feeding pipes 1 to the reactor 2 is 0.6-0.8; the diameter ratio of the diameter of the secondary branch pipe 5 to the diameter of the primary branch pipe 4 is 0.4-0.6; the diameter ratio of the diameter of the third-stage branch pipe 6 to the diameter of the second-stage branch pipe 5 is 0.3-0.5;

the first embodiment is as follows:

a vertical alkylation reaction device is used for preparing isooctane, the diameter of a reactor 2 is 4.4m, the diameter of a second feeding pipe 1 is 0.24m, the diameter of a first feeding pipe 3 is 0.5m, the diameter of a first-stage branch pipe 4 is 0.5m, the diameter of a second-stage branch pipe 5 is 0.22m, and the diameter of a third-stage branch pipe 6 is 0.07 m; the number of the second-stage branch pipes 5 is 6, the number of the third-stage branch pipes 6 is 36, and the number of the through holes 7 formed in the third-stage branch pipes 6 is 36. In this embodiment, hydrocarbon material is fed through the second feeding pipes 1 on both sides, acid material is fed through the first feeding pipe 3 in the middle, and both materials are converged in the first-stage branch pipe 4 through pipeline circulation and are uniformly mixed. The mixed material in the first-level branch pipe 4 uniformly distributes and flows into 6 second-level branch pipes 5, and further fully mixes in the second-level branch pipes 5. The mixed material is then divided into several small streams which flow into 36 three-stage branch pipes 6, respectively. And finally, spraying the small streams of material through 36 through holes 7 uniformly distributed on a three-stage branch pipe 6 forming an included angle of 45 degrees with the horizontal plane, uniformly covering the space cross section of the whole reactor 2, and reacting.

Specifically, it can be seen from the analysis of the product in the reactor 2 by sampling and detection that the octane number of the product is 95 and the conversion rate of olefin is 92%.

The reaction device of the utility model has the advantages of simple structure, good mixed distribution effect and high space utilization rate. Two kinds of liquid are poured into reactor 2 from different independent pipelines respectively, converge in same branch pipe again, intensive mixing, after evenly distributed, the reposition of redundant personnel is multistage stranded little burst material, sprays through-hole 7 at last, evenly covers on the space cross-section of whole reactor 2, and the reaction carries out. The reactor 2 organically combines the material distribution area and the reaction area together, thereby better saving space, and simultaneously reforming the structure and simplifying the process on the premise of ensuring the sufficient and uniform distribution of the materials. And the material distribution area is shorter and more compact, the cost is lower, the byproducts are less, and the conversion rate is high.

The foregoing is a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of improvements and decorations can be made without departing from the principle of the present invention, and these improvements and decorations are also considered as the protection scope of the present invention.

Claims

1. The utility model provides a vertical alkylation reaction device, includes the reactor, connects the first inlet pipe and the parallel equidistant distribution of reactor feed inlet are in first inlet pipe both sides and with two second inlet pipes that the reactor feed inlet is connected, its characterized in that still includes: the lower ends of the two second feeding pipes are respectively vertical and extend to be connected with the lower end of the first feeding pipe; the first-stage branch pipe is connected with the lower end of the first feeding pipe; a plurality of secondary branch pipes which are transversely and uniformly distributed around the primary branch pipe, wherein one end of each secondary branch pipe is connected with the primary branch pipe, and the other end of each secondary branch pipe is connected with the inner wall of the reactor; a plurality of three-stage branch pipes are uniformly connected below the two-stage branch pipes, and a plurality of through holes which are uniformly distributed are formed in the inner walls of the three-stage branch pipes.

2. The vertical alkylation reaction device according to claim 1, wherein: the three-level branch pipes are uniformly distributed below the two-level branch pipes in pairs, and each included angle between each three-level branch pipe and the horizontal plane is 45 degrees.

3. The vertical alkylation reaction device according to claim 1, wherein: and the tail end of the primary branch pipe and the tail end of the secondary branch pipe are both provided with pipe caps.

4. A vertical alkylation reaction device according to any one of claims 1 to 3, wherein: the reactor diameter is 4.4m, the second inlet pipe diameter is 0.24m, first inlet pipe diameter is 0.5m, one-level branch pipe diameter is 0.5m, second grade branch pipe diameter is 0.22m, third grade branch pipe diameter is 0.07m, second grade branch pipe quantity is 6, and third grade branch pipe quantity is 36, and the through-hole figure that third grade branch pipe set up is 36.

5. The vertical alkylation reaction device according to claim 1, wherein: the diameter ratio of the diameter of the second feeding pipe to the diameter of the first feeding pipe is 0.5-0.6.

6. The vertical alkylation reaction device according to claim 1, wherein: the diameter ratio of the distance between the two second feeding pipes and the reactor is 0.6-0.8.

7. A vertical alkylation reaction apparatus according to claim 1 or 3, wherein: the diameter ratio of the diameter of the secondary branch pipe to the diameter of the primary branch pipe is 0.4-0.6.

8. A vertical alkylation reaction apparatus according to claim 1 or 2, wherein: the diameter ratio of the diameter of the third-stage branch pipe to the diameter of the second-stage branch pipe is 0.3-0.5.