CN219580522U

CN219580522U - Polymerization device for producing polybutene-1

Info

Publication number: CN219580522U
Application number: CN202320724437.4U
Authority: CN
Inventors: 董月梅; 逯云峰; 李志鹏; 曹坚; 陈意心; 安振永; 邹明华
Original assignee: Beijing Petrochemical Engineering Co Ltd
Current assignee: Beijing Petrochemical Engineering Co Ltd
Priority date: 2023-04-04
Filing date: 2023-04-04
Publication date: 2023-08-25
Anticipated expiration: 2033-04-04

Abstract

The utility model discloses a polymerization device for producing polybutene-1, which comprises a reaction kettle, an internal cooling device arranged in the reaction kettle, and further comprises: the cooling heat exchanger is connected with a first discharge hole at the lower end of the reaction kettle; the first mixture in the reaction kettle is returned to the reaction kettle in a liquid state through the cooling heat exchanger. The method comprises the steps of arranging a cooling heat exchanger outside the reaction kettle, flowing the first mixture in the reaction kettle into the cooling heat exchanger in a liquid form, cooling in the cooling heat exchanger, then introducing the cooled first mixture into the reaction kettle, cooling the first mixture in the reaction kettle outside the reaction kettle, and controlling the temperature in the reaction kettle. The heat exchange efficiency of the polybutene-1 polymerization kettle is improved by adopting a mode of combining an external cooling heat exchanger with an internal cooling device, and the operation efficiency and the profit of equipment are improved. Prevent the phenomena of catalyst deactivation, product property change and the like caused by overhigh temperature in the kettle, and ensure the production scale and the product quality.

Description

Polymerization device for producing polybutene-1

Technical Field

The utility model relates to the technical field of high polymer materials, in particular to a polymerization device for producing polybutene-1.

Background

Polybutene-1 has excellent creep resistance, impact resistance, stress resistance and other performances, has excellent chemical stability, is environment-friendly, is a good material for manufacturing pipes, and can be used as a packaging film material for medical treatment and food. In recent years, the demand of polybutene-1 in China is increased year by year, and the existing polybutene-1 polymerization kettles are usually provided with tubular heat exchange devices in the kettles for heat exchange, so that the reaction temperature in the polymerization kettles is controlled. The proposal has limited heat exchange capacity, and in the production process, phenomena such as catalyst deactivation, product property change and the like caused by temperature runaway easily occur in a polymerization kettle, thereby severely limiting the production scale and the product quality.

Disclosure of Invention

The present utility model aims to solve at least one of the technical problems existing in the prior art. To this end, the present utility model proposes a polymerization apparatus for producing polybutene-1, which is capable of sufficiently cooling reactants, products and catalyst in a polymerization apparatus for producing polybutene-1 by providing a cooling heat exchanger outside a reaction vessel.

The polymerization device for producing polybutene-1 according to the embodiment of the present utility model comprises a reaction kettle, an internal cooling device arranged inside the reaction kettle, and further comprises: the cooling heat exchanger is connected with a first discharge hole at the lower end of the reaction kettle; the first mixture in the reaction kettle is returned to the reaction kettle in a liquid state through the cooling heat exchanger.

In some embodiments, the first mixture includes a liquid reactant, a liquid product, and a liquid catalyst within the reaction vessel.

Further, the reaction kettle further comprises: the second discharging hole is used for discharging a second mixture and is arranged at the upper end of the reaction kettle.

Further, the second mixture comprises a liquid product and a liquid reactant.

In some embodiments, the reaction kettle is further connected with a first feed line, a second feed line, and a return line; the liquid reactant enters the reaction kettle through the first feeding pipeline; the liquid catalyst enters the reaction kettle through the second feeding pipeline; the first mixture in the cooling heat exchanger is returned to the reaction kettle through the return pipeline.

Further, the liquid reactant is a mixture of butene-1 and hexane, and the ratio of butene-1 to hexane in the first feed line I is at 40:1 to 40:1.5, the feeding pressure of the liquid reactant is 2-2.5 MP, and the feeding temperature is 60-65 ℃.

In some embodiments, the liquid catalyst comprises a catalyst and a promoter, the ratio of the catalyst to the promoter in the second feed line being 1:33 to 1.2: 33.

In some embodiments, the feed ratio of the liquid reactant and the liquid catalyst is 2500:1 to 2600: 1.

In some embodiments, the concentration of the liquid product in the first mixture ranges between 10 and 30%; in the second mixture, the concentration of the liquid product ranges from 30% to 35%.

In some embodiments, the pressure inside the reaction vessel is between 1.5 and 3.5MPa and the temperature is between 70 and 80 ℃.

The utility model relates to a polymerization device for producing polybutene-1, wherein a cooling heat exchanger is arranged outside a reaction kettle, a first mixture in the reaction kettle flows into the cooling heat exchanger in a liquid form, is cooled in the cooling heat exchanger and then is introduced into the reaction kettle, the first mixture in the reaction kettle is cooled outside the reaction kettle, and the temperature in the reaction kettle is controlled. The heat exchange efficiency of the polybutene-1 polymerization kettle is improved by adopting a mode of combining an external cooling heat exchanger with an internal cooling device, and the operation efficiency and the profit of equipment are improved. Prevent the phenomena of catalyst deactivation, product property change and the like caused by overhigh temperature in the kettle, and ensure the production scale and the product quality.

Drawings

In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are needed in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present utility model, and other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.

FIG. 1 is a schematic view of a polymerization apparatus for producing polybutene-1 according to the present embodiment.

Reference numerals:

a polymerization device 100 for producing polybutene-1, a reaction kettle 10, an internal cooling device 20, a cooling heat exchanger 30, a stirrer 41, a driver 42, a first feeding pipeline I, a second feeding pipeline II, a second discharging port III, a first discharging port IV and a return pipeline V.

Detailed Description

The description of the embodiments of this specification should be taken in conjunction with the accompanying drawings, which are a complete description of the embodiments. In the drawings, the shape or thickness of the embodiments may be enlarged and indicated simply or conveniently. Furthermore, portions of the structures in the drawings will be described in terms of separate descriptions, and it should be noted that elements not shown or described in the drawings are in a form known to those of ordinary skill in the art.

Any references to directions and orientations in the description of the embodiments herein are for convenience only and should not be construed as limiting the scope of the utility model in any way. The following description of the preferred embodiments will refer to combinations of features, which may be present alone or in combination, and the utility model is not particularly limited to the preferred embodiments. The scope of the utility model is defined by the claims.

A polymerization apparatus 100 for producing polybutene-1 according to embodiments of the present utility model will be described below with reference to fig. 1.

As shown in fig. 1, a polymerization apparatus 100 for producing polybutene-1 according to an embodiment of the present utility model includes: a reaction kettle 10, an internal cooling device 20 and a cooling heat exchanger.

The stirring device is arranged in the reaction kettle 10 and comprises a stirrer 41 and a driver 42, and the driver 42 drives the stirring device to periodically stir in the reaction kettle 10, so that mutual contact between auxiliary reactants and catalytic substances is facilitated, the reaction rate is improved, the reactants are fully reacted, the reactant waste is reduced, the production cost is reduced, and meanwhile, the reactants mixed in the products are reduced, so that convenience is brought to subsequent purification of the products.

The internal cooling device 20 is arranged in the reaction kettle 10 and is used for cooling reactants, catalytic substances and products in the reaction kettle 10. The temperature in the reaction kettle 10 is reduced, and the polymerization reaction in the reaction kettle 10 can be maintained to be normally carried out.

The internal cooling device is arranged as a tube type heat exchanger in the reactor, the number of the tube type heat exchangers can be multiple, and the tube type heat exchangers are uniformly arranged on the inner wall of the reactor in a surrounding mode at intervals.

The lower end of the reaction kettle 10 is provided with a first discharge port IV which is connected with a cooling heat exchanger 30 arranged outside the reaction kettle 10. The first mixture in the reaction kettle 10 flows out from the first discharge port IV in a liquid state, is cooled by the cooling heat exchanger 30, and then returns to the reaction kettle 10, and the temperature reduction range of the first mixture cooled by the cooling heat exchanger 30 is 20-25 ℃. It is understood that the first mixture is circulated between the cooling heat exchanger and the reaction kettle, the first mixture includes reactant and product of the reactant, and the first reactant is in liquid form, so that the first discharging port is set in the lower end of the reaction kettle.

The cooling heat exchanger 30 may selectively use cooling water as a cooling medium, but not limited to this, and the cooling medium may be adjusted according to different situations in the actual production process.

It can be understood that the conventional polybutene-1 reaction kettle 10 is usually provided with a tube array heat exchange device in the kettle for heat exchange and cooling, so as to control the reaction temperature in the reaction kettle 10. The proposal has limited heat exchange capacity, and during the production process, phenomena such as catalyst deactivation, product property change and the like are easy to occur in the reaction kettle 10, thereby severely limiting the production scale and the product quality.

In order to solve the above problems, the present utility model proposes a polymerization apparatus 100 for producing polybutene-1, which can control the reaction temperature in the reaction kettle 10 as much as possible by using the structure thereof, and effectively avoid the problems of catalyst deactivation, product property change, etc. caused by the occurrence of the temperature runaway in the reaction kettle 10.

Specifically, a cooling heat exchanger 30 is arranged outside the reaction kettle 10, the first mixture in the reaction kettle 10 flows into the cooling heat exchanger 30 in a liquid form, is cooled in the cooling heat exchanger 30 and then is introduced into the reaction kettle 10, the first mixture in the reaction kettle 10 is cooled outside the kettle, and the temperature in the reaction kettle 10 is controlled. The heat exchange efficiency of the polybutene-1 polymerizer is improved by adopting a mode of combining the external cooling heat exchanger 30 and the internal cooling device 20, and the operation efficiency and the profit of the equipment are improved. Prevent the phenomena of catalyst deactivation, product property change and the like caused by overhigh temperature in the kettle, ensure the product quality, and be favorable for ensuring the production scale on the basis. Ensures the high quality and the improvement of the yield of the polybutene-1 product and lower cost, and can effectively ensure the full play of the social benefit and the economic benefit.

In some embodiments, the first mixture includes a liquid reactant, a liquid product, and a liquid catalyst within the reaction vessel 10.

The temperature of the first mixture formed by mixing the liquid reactant, the liquid product and the liquid catalyst in the reaction kettle 10 is higher, the reaction operation efficiency in the reaction kettle 10 is affected, the liquid reactant, the liquid product and the liquid catalyst in the first mixture are cooled by introducing the first mixture into the cooling heat exchanger 30 from the first discharge port IV, and meanwhile, an internal cooling device is arranged in the reaction kettle and is matched with the cooling heat exchanger, so that the liquid reactant and the liquid catalyst are maintained at a temperature suitable for reaction. The ratio of liquid reactant to liquid catalyst in the first mixture is the same as the feed ratio.

Further, the reaction vessel 10 further includes: the second discharging hole III is used for discharging the second mixture and is arranged at the upper end of the reaction kettle 10.

The material conversion rate near the top of the reaction kettle is higher, so that a large amount of liquid products are arranged at the top of the reaction kettle 10, a second mixture is formed by combining a large amount of liquid products and less liquid products after reaction, materials in the reaction kettle 10 are gradually increased to be removed in the process of continuously introducing reactants and generating the products by reaction, the materials leave the reaction kettle from the top of the reaction kettle and enter a subsequent working section, and the second mixture overflows through a second discharge port III, so that the second discharge port III arranged at the upper end of the reaction kettle 10 can discharge the second mixture in a liquid state out of the reaction kettle 10, and the simultaneous discharge of the liquid first mixture is prevented.

The liquid product is mixed with liquid reactant to form a second mixture, the second mixture is discharged out of the reaction kettle 10 through a second discharge port III, the liquid product is a product polybutene-1, and the liquid reactant is partially unreacted butene-1 and hexane.

In some embodiments, the reaction kettle 10 is further connected with a first feeding pipeline I, a second feeding pipeline II and a return pipeline; the liquid reactant enters the reaction kettle 10 through a first feeding pipeline I; the liquid catalyst enters the reaction kettle 10 through a second feeding pipeline II; the first mixture in the cooling heat exchanger 30 is returned to the reaction tank 10 through a return line V.

Wherein, the feed back pipeline can set up the position in the upper end of reation kettle, also can set up the position in reation kettle lower extreme.

The liquid reactant enters the reaction kettle 10 through the first feeding pipeline I, and the liquid catalyst enters the reaction kettle 10 through the second feeding pipeline II, so that the liquid reactant and the liquid catalyst are not contacted with each other before entering the reaction kettle 10, and the liquid reactant and the liquid catalyst are not contacted and react until entering the reaction kettle 10. The first mixture in the cooling heat exchanger 30 is returned to the reactor 10 via the return line V to ensure that the first mixture does not come into contact with the newly fed liquid reactant and liquid catalyst before entering the reactor 10. The reaction is prevented from occurring in the feed line resulting in damage to the feed line.

Further, the liquid reactant is a mixture of butene-1 and hexane, and the ratio of butene-1 to hexane in the first feed line I is 40:1 to 40:1.5, the feeding pressure of the liquid reactant is 2-2.5 MP, and the feeding temperature is 60-65 ℃.

The ratio of butene-1 to hexane was 40:1 to 40: the polymerization reaction raw materials can be fully utilized between 1.5, the reaction efficiency is highest, and the butene-1 and hexane can be ensured to be kept in a liquid state when the feeding pressure is 2-2.5 MP and the feeding temperature is 60-65 ℃, so that reactants can be fused better. The reaction is carried out under the pressure and the temperature, so that the reaction efficiency of the reaction is ensured.

In some embodiments, the liquid catalyst comprises catalyst and promoter in a ratio of 1:33 to 1.2: 33.

For example, the catalyst may be TiCl4/MgCl2 supported catalyst and the promoter may be triethylaluminum cocatalyst.

In some embodiments, the feed ratio of liquid reactant to liquid catalyst is 2500:1 to 2600: 1.

The proportion is 2500:1 to 2600: and 1, the liquid catalyst can ensure the catalytic efficiency and simultaneously save the use of the liquid catalyst, so that the polymerization reaction of the polybutene-1 is more economical.

In some embodiments, the concentration of the liquid product in the first mixture ranges between 10 and 30%; in the second mixture, the concentration of the liquid product is in the range of 30-35%.

In the second mixture, the concentration range of the liquid product is between 30 and 35 percent, so that the subsequent extraction and separation of the liquid product can be more convenient, and the quality and yield of the liquid product are ensured.

In some embodiments, the pressure inside the reactor 10 is between 1.5 and 3.5MPa and the temperature is between 70 and 80 ℃.

The pressure is between 1.5 and 3.5MPa, the temperature is between 70 and 80 ℃, and the pressure and the temperature are the most suitable for the reaction of internal reactants, so that the reaction efficiency in the reaction kettle 10 is the highest, and the running efficiency and the profit of equipment are improved. Prevent the phenomena of catalyst deactivation, product property change and the like caused by overhigh temperature in the kettle, and ensure the production scale and the product quality.

The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.

Claims

1. A polymerization plant for producing polybutene-1, includes reation kettle (10), sets up interior cold charge (20) in reation kettle (10) inside, its characterized in that still includes:

a cooling heat exchanger (30) connected with a first discharge port (IV) at the lower end of the reaction kettle (10);

the first mixture in the reaction kettle (10) returns to the reaction kettle (10) in a liquid state through the cooling heat exchanger (30).

2. The polymerization apparatus for producing polybutene-1 according to claim 1, characterized in that the first mixture comprises a liquid reactant, a liquid product and a liquid catalyst in the reaction vessel (10).

3. The polymerization apparatus for producing polybutene-1 according to claim 2, characterized in that the reaction vessel (10) further comprises:

the second discharging hole (III) is used for discharging a second mixture, and the second discharging hole (III) is arranged at the upper end of the reaction kettle (10).

4. A polymerization apparatus for producing polybutene-1 according to claim 3 characterised in that said second mixture comprises liquid product, liquid reactant.

5. The polymerization apparatus for producing polybutene-1 according to claim 2, characterized in that the reaction vessel (10) is further connected with a first feed line (I), a second feed line (II) and a return line (V); the liquid reactant enters the reaction kettle (10) through the first feeding pipeline (I); the liquid catalyst enters the reaction kettle (10) through the second feeding pipeline (II); the first mixture in the cooling heat exchanger (30) is returned to the reaction kettle (10) through the return pipeline (V).