CN219186864U

CN219186864U - System for producing high-purity n-butane and co-producing high-purity 1-butene through carbon four after ether

Info

Publication number: CN219186864U
Application number: CN202320639151.6U
Authority: CN
Inventors: 王来珅; 李玉香; 张宝; 李本锋
Original assignee: Zibo Hai Yi Fine Chemical Co ltd
Current assignee: Zibo Hai Yi Fine Chemical Co ltd
Priority date: 2023-03-28
Filing date: 2023-03-28
Publication date: 2023-06-16
Anticipated expiration: 2033-03-28

Abstract

The utility model discloses a system for producing high-purity n-butane and co-producing high-purity 1-butene by using carbon four after ether, belonging to the technical field of petrochemical industry. The technical proposal is as follows: comprises a dimethyl ether removing tower, a C5 removing tower, a solvent extracting tower, a stripping tower, an n-butane tower, an isobutane tower, a orthosteric unit, a carbon four hydrogenation reactor, a 1-butene separating tower and a carbon four olefin skeleton isomerization reactor; the dimethyl ether removal tower is provided with an after-ether carbon four inlet pipeline and a light component outlet pipeline, and the n-butane outlet of the carbon four hydrogenation reactor is connected with a refined n-butane maleic anhydride removal pipeline; the bottom outlet of the solvent extraction tower is sequentially connected with a stripping tower, a 1-butene separation tower and a carbon tetraolefin skeleton isomerization reactor through pipelines, and the 1-butene separation tower is connected with a 1-butene outlet pipeline; the mixed n-isobutane outlet of the n-structuring unit is communicated with the mixed n-isobutane inlet of the n-butane tower through a pipeline. The utility model produces high-purity butane and coproduces high-purity 1-butene, and solves the difficulty of high-value utilization of the carbon four after the prior ether.

Description

System for producing high-purity n-butane and co-producing high-purity 1-butene through carbon four after ether

Technical Field

The utility model relates to the technical field of petrochemical industry, in particular to a system for producing high-purity n-butane and co-producing high-purity 1-butene through carbon four after ether.

Background

The liquefied gas products in petrochemical industry and coal chemical industry are separated into propane, propylene and carbon four products after gas separation, wherein the propane is used as fuel, the propylene is used as chemical products, but the carbon four products mainly used as MTBE and alkylate oil because of containing a large amount of carbon four olefins and carbon four alkanes. Due to development of electric automobiles and implementation of carbon emission policies, gasoline sales are lower and lower, so that the alkylated oil market is gradually excessive, and economic benefits are poorer and worse. And a large amount of carbon four products after ether are used as low-price fuel gas in the market, so that huge waste is caused. The separation of high-purity n-butane, isobutane and 1-butene from the post-ether carbon four is becoming the focus of market attention more and more as raw materials for downstream chemical products.

The ether carbon four mainly comprises n-butane, isobutane, cis-butene, trans-butene, 1-butene and the like, wherein each high-purity component is a good chemical raw material. Wherein n-butane is the raw material of a maleic anhydride device, a degradable plastic PBS (Poly Butylene succinate) and the like are produced at the downstream of maleic anhydride, 1-butene is a comonomer of polyethylene, and 2-butene is the raw material of methyl ethyl ketone. However, the carbon four after the ether contains a series of impurities such as dimethyl ether, methanol, isobutene, butadiene and the like, which causes a certain difficulty for subsequent deep processing. Meanwhile, the boiling points of n-butane, isobutane, cis-butene, trans-butene, 1-butene, isobutene, butadiene and the like are close, and separation is difficult to carry out by a common rectification mode. Therefore, how to remove impurities in the etherified carbon four and produce high-purity n-butane and coproduce high-purity 1-butene is a problem of high-value utilization of the existing etherified carbon four.

Disclosure of Invention

The utility model aims to solve the technical problems that: overcomes the defects of the prior art, provides a system for producing high-purity n-butane and co-producing high-purity 1-butene by using the carbon four after the ether, and solves the difficulty of high-value utilization of the carbon four after the ether.

The technical scheme of the utility model is as follows: a system for producing high-purity n-butane and co-producing high-purity 1-butene by using etherified carbon four comprises a dimethyl ether removal tower, a C5 removal tower, a solvent extraction tower, a stripping tower, an n-butane tower, an isobutane tower, an orthosteric unit, a carbon four hydrogenation reactor, a 1-butene separation tower and a carbon four olefin skeleton isomerization reactor; the dimethyl ether removal tower is sequentially connected with a C5 removal tower, a solvent extraction tower, a n-butane tower and a carbon four hydrogenation reactor through pipelines, the dimethyl ether removal tower is provided with a carbon four inlet pipeline after ether and a light component outlet pipeline, and the n-butane outlet of the carbon four hydrogenation reactor is connected with a refined n-butane maleic anhydride removal pipeline; the bottom outlet of the solvent extraction tower is sequentially connected with a stripping tower, a 1-butene separation tower and a carbon tetraolefin skeleton isomerization reactor through pipelines, and the 1-butene separation tower is connected with a 1-butene outlet pipeline; the C5 removing tower is provided with a C5 outlet pipeline I, and the C5 outlet pipeline I is connected with a C5 tank area; the n-butane tower is provided with a second C5 outlet pipeline, and the second C5 outlet pipeline is connected with a C5 tank area; the stripping tower is provided with a regenerated solvent outlet pipeline which is communicated with a reflux solvent inlet of the solvent extraction tower; the n-butane tower is provided with an isobutane outlet pipeline, the isobutane outlet pipeline is connected with an inlet of the isobutane tower, an outlet at the top of the isobutane tower is connected with a orthographic unit through a pipeline, and an outlet of the orthographic unit is connected with a carbon four hydrogenation reactor through a pipeline; the mixed n-isobutane outlet of the n-structuring unit is communicated with the mixed n-isobutane inlet of the n-butane tower through a pipeline; the bottom material outlet of the isobutane tower is communicated with the material inlet of the n-butane tower through a pipeline; the carbon tetraolefin skeleton isomerization reactor is provided with a C5 and above component outlet pipeline.

Preferably, a reboiler is arranged between the dimethyl ether removing tower and the C5 removing tower.

Compared with the prior art, the utility model has the following beneficial effects:

the utility model provides a system for producing high-purity n-butane and co-producing high-purity 1-butene by using four carbon atoms after ether, which can produce high-purity n-butane and co-produce high-purity 1-butene, solves the problem of high-value utilization of the four carbon atoms after ether, extends the industrial chain of four carbon atoms after ether, improves the added value of four carbon atoms after ether, and simultaneously effectively reduces the energy consumption and the material consumption of a device.

Drawings

Fig. 1 is a schematic structural view of the present utility model.

In the figure, a dimethyl ether removing tower is shown as the specification; 101. a post-ether carbon four inlet line; 102. a light component outlet line; 2. a reboiler; 3. a C5 removing tower; 301. c5 outlet line one; 302. a C5 tank farm; 4. a solvent extraction column; 401. a solvent extraction column reflux solvent inlet; 5. a stripping column; 501. a regenerated solvent outlet line; 6. a n-butane tower; 601. an isobutane outlet line; 602. a mixed n-isobutane inlet; 603. c5 outlet pipeline II; 7. an isobutane tower; 701. an isobutane column inlet; 8. a orthosteric unit; 801. a mixed n-isobutane outlet; 9. a carbon four hydrogenation reactor; 901. an n-butane outlet; 902. a maleic anhydride removing pipeline for refining n-butane; 10. a 1-butene separation column; 1001. a 1-butene outlet line; 11. a carbon tetraolefin skeletal isomerization reactor; 1101. c5 and above component outlet line.

Detailed Description

The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.

Example 1

As shown in fig. 1, the embodiment provides a system for producing high-purity n-butane and co-producing high-purity 1-butene by using four carbon atoms after ether, which comprises a dimethyl ether removal tower 1, a C5 removal tower 3, a solvent extraction tower 4, a stripping tower 5, an n-butane tower 6, an isobutane tower 7, an orthostructurization unit 8, a four carbon hydrogenation reactor 9, a 1-butene separation tower 10 and a four carbon olefin skeleton isomerization reactor 11; the dimethyl ether removal tower 1 is sequentially connected with a C5 removal tower 3, a solvent extraction tower 4, a normal butane tower 6 and a C5 removal hydrogenation reactor 9 through pipelines, a reboiler 2 is arranged between the dimethyl ether removal tower 1 and the C5 removal tower 3, the dimethyl ether removal tower 1 is provided with a post-ether C5 inlet pipeline 101 and a light component outlet pipeline 102, and a normal butane outlet 901 of the C5 removal hydrogenation reactor 9 is connected with a refined normal butane maleic anhydride removal pipeline 902; the bottom outlet of the solvent extraction tower 4 is sequentially connected with a stripping tower 5, a 1-butene separation tower 10 and a carbon four-olefin skeletal isomerization reactor 11 through pipelines, and the 1-butene separation tower 10 is connected with a 1-butene outlet pipeline 1001; the C5 removing tower 3 is provided with a first C5 outlet pipeline 301, and the first C5 outlet pipeline 301 is connected with a C5 tank area 302; the n-butane tower 6 is provided with a second C5 outlet pipeline 603, and the second C5 outlet pipeline 603 is connected with the C5 tank area 302; the stripping tower 5 is provided with a regenerated solvent outlet pipeline 501, and the regenerated solvent outlet pipeline 501 is communicated with the reflux solvent inlet 401 of the solvent extraction tower; the n-butane tower 6 is provided with an isobutane outlet pipeline 601, the isobutane outlet pipeline 601 is connected with an isobutane inlet 701, the top outlet of the isobutane tower 7 is connected with a orthosteric unit 8 through a pipeline, and the outlet of the orthosteric unit 8 is connected with a four-carbon hydrogenation reactor 9 through a pipeline; the mixed n-isobutane outlet 801 of the orthosteric unit 8 is communicated with the mixed n-isobutane inlet 602 of the n-butane tower 6 through a pipeline; the bottom material outlet of the isobutane tower 7 is communicated with the material inlet of the n-butane tower 6 through a pipeline; the carbon tetraolefin skeletal isomerization reactor 11 is provided with a C5 and above component outlet line 1101.

The working process comprises the following steps: the carbon four after the ether enters a dimethyl ether removal tower 1 through a carbon four after the ether inlet pipeline 101, the carbon four after the ether contains components such as dimethyl ether, methanol, MTBE, C5 and the like, the light components such as dimethyl ether, carbon three, methanol and the like are removed from the carbon four after the ether through the dimethyl ether removal tower 1 in sequence in a common rectification mode, the heavy components such as MTBE, C5 and the like are removed from the carbon four after the ether through a decarburization five tower, C5 enters a C5 tank area 302 through a C5 outlet pipeline 301, and purified C4 enters a solvent extraction tower 4; the decarbonization five-tower and the dimethyl ether removal tower 1 realize the thermal coupling utilization, the specific method is to moderately increase the pressure and the temperature of the C5 removal tower 3, one part of the gas phase at the top of the tower is directly used for heating by a reboiler 2 at the kettle of the dimethyl ether removal tower 1, and the other part of the gas phase at the top of the tower directly enters the solvent extraction tower 4 without cooling. The gas phase at the top of the tower not only realizes the utilization of heat, but also omits the cooling load of a water cooler, and greatly reduces the energy consumption.

The C4 gas phase after the ether is purified by the C5 tower 3 enters a solvent extraction tower 4, the mixed butane of the isobutane and the n-butane is obtained at the top of the tower under the extraction and separation action of the solvent, and the mixture of the solvent and the butene is obtained at the bottom of the tower; mixing n-isobutane, entering a n-butane tower 6, obtaining an isobutane product at the top of the n-butane tower 6, extracting n-butane from the side line of the n-butane tower 6, obtaining heavy components such as C5 at the bottom of the n-butane tower 6, entering a C5 tank area 302 through a C5 outlet pipeline II 603, and adopting a lean solvent with residual low-temperature heat of an extraction rectifying tower and residual hot water of a factory as heating sources at the temperature of 64 ℃ at the bottom of the n-butane tower 6.

In order to prevent possible fluctuation of olefin content in the n-butane, the n-butane product from the n-butane tower 6 enters a hydrogenation saturation unit, ensures the quality of the n-butane as a maleic anhydride raw material, and obtains the n-butane product with 99% purity. A small amount of C4 carried in the hydrogen discharged from the hydrogenation stabilization tower top of the hydrogenation saturation unit can enter a C3 removal tower or a dimethyl ether removal tower 1 for recycling, and a small amount of hydrogen enters a fuel gas pipe network.

The isobutane product separated by the normal butane tower 6 is further purified by the isobutane tower 7 and enters the normal butane unit 8 to carry out normal formation reaction, the single-pass conversion rate is about 35%, the total conversion rate is more than 95%, the normal formation reaction unit comprises two fixed bed reactors and a heating furnace, and normal isobutane generated by the reaction returns to the normal butane tower 6.

The mixture of the solvent and the butene from the solvent extraction tower 4 enters a stripping tower 5, mixed butene is obtained at the top of the stripping tower 5, the bottom solvent is recycled by a series of heat recovery and then returned to the solvent extraction tower 4, the mixed butene enters a 1-butene separation tower 10 for 1-butene separation, 2-butene from the 1-butene separation tower 10 enters a butene framework normal unit for producing 1-butene, the produced 1-butene enters the 1-butene separation tower 10 again for recycling, the reaction condition is 200-300 ℃, the single pass conversion rate is 15-20%, the total conversion rate is 50-70%, and finally the 1-butene product with the purity of 99.6%, the small amount of 2-butene product and the small amount of heavy components with the yield of about 80% are obtained.

Although the present utility model has been described in detail by way of preferred embodiments with reference to the accompanying drawings, the present utility model is not limited thereto. Various equivalent modifications and substitutions for embodiments of the utility model may be made by those skilled in the art without departing from the spirit and scope of the utility model, and these modifications and substitutions are intended to be within the scope of the utility model. Therefore, the protection scope of the present utility model shall be subject to the protection scope of the claims.

Claims

1. A system for producing high-purity n-butane and co-producing high-purity 1-butene by using carbon four after ether is characterized in that: comprises a dimethyl ether removing tower (1), a C5 removing tower (3), a solvent extracting tower (4), a stripping tower (5), an n-butane tower (6), an isobutane tower (7), a orthostatic unit (8), a carbon four hydrogenation reactor (9), a 1-butene separating tower (10) and a carbon four olefin skeleton isomerization reactor (11);

the dimethyl ether removal tower (1) is sequentially connected with a C5 removal tower (3), a solvent extraction tower (4), a n-butane tower (6) and a carbon four hydrogenation reactor (9) through pipelines, the dimethyl ether removal tower (1) is provided with a carbon four inlet pipeline (101) after ether and a light component outlet pipeline (102), and a n-butane outlet (901) of the carbon four hydrogenation reactor (9) is connected with a refined n-butane maleic anhydride removal pipeline (902);

the bottom outlet of the solvent extraction tower (4) is sequentially connected with a stripping tower (5), a 1-butene separation tower (10) and a carbon tetraolefin skeleton isomerization reactor (11) through pipelines, and the 1-butene separation tower (10) is connected with a 1-butene outlet pipeline (1001);

the C5 removing tower (3) is provided with a C5 outlet pipeline I (301), and the C5 outlet pipeline I (301) is connected with a C5 tank area (302);

the n-butane tower (6) is provided with a C5 outlet pipeline II (603), and the C5 outlet pipeline II (603) is connected with the C5 tank area (302);

the stripping tower (5) is provided with a regenerated solvent outlet pipeline (501), and the regenerated solvent outlet pipeline (501) is communicated with a reflux solvent inlet (401) of the solvent extraction tower;

the n-butane tower (6) is provided with an isobutane outlet pipeline (601), the isobutane outlet pipeline (601) is connected with an isobutane tower inlet (701), the top outlet of the isobutane tower (7) is connected with a orthogonalization unit (8) through a pipeline, and the outlet of the orthogonalization unit (8) is connected with a carbon four hydrogenation reactor (9) through a pipeline;

the mixed n-isobutane outlet (801) of the orthographic structuring unit (8) is communicated with the mixed n-isobutane inlet (602) of the n-butane tower (6) through a pipeline;

the bottom material outlet of the isobutane tower (7) is communicated with the material inlet of the n-butane tower (6) through a pipeline;

the carbon tetraolefin skeleton isomerization reactor (11) is provided with a C5 and above component outlet pipeline (1101).

2. The system for producing high-purity n-butane and co-producing high-purity 1-butene by using carbon four after ether according to claim 1, wherein: a reboiler (2) is arranged between the dimethyl ether removal tower (1) and the C5 removal tower (3).