CN213506663U - Separation recovery system of cyclohexanol technology raw materials - Google Patents
Separation recovery system of cyclohexanol technology raw materials Download PDFInfo
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- CN213506663U CN213506663U CN202022158483.1U CN202022158483U CN213506663U CN 213506663 U CN213506663 U CN 213506663U CN 202022158483 U CN202022158483 U CN 202022158483U CN 213506663 U CN213506663 U CN 213506663U
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Abstract
The utility model provides a separation recovery system of cyclohexanol technology raw materials, including benzene knockout tower, cyclohexene knockout tower, hydrogenation unit, it is first, the second rectifying column, the top of the tower bin outlet of benzene knockout tower is through first condenser, first buffer tank, to the feed of cyclohexene knockout tower, the top of the tower bin outlet of cyclohexene knockout tower is through second condenser, the second buffer tank, to the hydrogenation unit feed, the bin outlet of hydrogenation unit is to the feed of first rectifying column, the top of the tower bin outlet of first rectifying column is through third condenser, the third buffer tank, to the feed of second rectifying column, the top of the tower bin outlet of second rectifying column is through fourth condenser, the fourth buffer tank, to the feed of light component jar. The utility model has the advantages of being simple in structure and convenient in operation, can effectively separate the raw materials of cyclohexanol technology, and retrieve impurity wherein.
Description
Technical Field
The utility model relates to a chemical industry field, in particular to separation recovery system of cyclohexanol technology raw materials.
Background
Cyclohexanol is an organic compound, is a viscous liquid at normal temperature and pressure, and is an important raw material for preparing adipic acid. Benzene is usually adopted as a raw material in chemical enterprises, cyclohexene and cyclohexane are obtained by hydrogenation in a benzene hydrogenation device, the separated cyclohexene is used as a raw material for synthesizing cyclohexanol after separation, a target product of the cyclohexanol is obtained by hydration, and the separated cyclohexane is used as a raw material of a plant oxidation device.
However, in the separation process of cyclohexene and cyclohexane obtained by benzene hydrogenation, the separated cyclohexane inevitably contains a small amount of cyclohexene and benzene, and by-product impurities, and if the cyclohexene and cyclohexane are directly used as raw materials, the impurities can affect the quality of downstream products and cause serious waste of the impurities.
Disclosure of Invention
The utility model aims at prior art not enough, provide a separation recovery system of cyclohexanol technology raw materials, its simple structure, convenient operation can effectively separate the raw materials of cyclohexanol technology, and retrieve impurity wherein.
The technical scheme of the utility model is that: a separation and recovery system of cyclohexanol process raw materials comprises a benzene separation tower, a cyclohexene separation tower, a hydrogenation device, a first rectification tower and a second rectification tower, wherein a feed inlet of the benzene separation tower is used for being connected with the benzene hydrogenation device, a discharge outlet at the top of the benzene separation tower supplies materials to the cyclohexene separation tower through a first condenser and a first buffer tank, a discharge outlet at the bottom of a tower kettle of the benzene separation tower supplies materials to the cyclohexene tank, a discharge outlet at the top of the cyclohexene separation tower supplies materials to the hydrogenation device through a second condenser and a second buffer tank, a discharge outlet at the bottom of the tower of the cyclohexene separation tower supplies materials to the cyclohexene tank, a discharge outlet of the hydrogenation device supplies materials to the first rectification tower through a third pipeline, a discharge outlet at the top of the first rectification tower supplies materials to the second rectification tower through a third condenser and a third buffer tank, and a discharge outlet at the bottom of the first rectification tower supplies materials to the cyclohexane tank through a fourth pipeline, and a tower top discharge port of the second rectifying tower supplies materials to the light component tank through a fifth pipeline through a fourth condenser and a fourth buffer tank, and a tower kettle discharge port of the second rectifying tower supplies materials to the cyclohexane tank.
The first pipeline is provided with a first material conveying pump and a first valve, and the first valve is positioned at the downstream of the first material conveying pump.
The benzene separation tower is characterized by further comprising a first return pipe, the upstream end of the first return pipe is connected with the first pipeline and located between the first material conveying pump and the first valve, the downstream end of the first return pipe is connected with the upper portion of the side wall of the benzene separation tower, and the first return pipe is provided with a second valve.
And a second material conveying pump and a third valve are arranged on the second pipeline, and the third valve is positioned at the downstream of the second material conveying pump.
The device is characterized by further comprising a second return pipe, the upstream end of the second return pipe is connected with a second pipeline and located between a second material conveying pump and a third valve, the downstream end of the second return pipe is connected with the upper portion of the side wall of the cyclohexene separation tower, and a fourth valve is arranged on the second return pipe.
And a third material conveying pump and a fifth valve are arranged on the fourth pipeline, and the fifth valve is positioned at the downstream of the third material conveying pump.
The third reflux pipe is connected with a fourth pipeline at the upstream end and is positioned between the third material conveying pump and the fifth valve, the downstream end is connected with the upper part of the side wall of the first rectifying tower, and the third reflux pipe is provided with a sixth valve.
And a fourth material conveying pump and a seventh valve are arranged on the fifth pipeline, and the seventh valve is positioned at the downstream of the fourth material conveying pump.
The upstream end of the fourth return pipe is connected with the fifth pipeline and is positioned between the fourth material conveying pump and the seventh valve, the downstream end of the fourth return pipe is connected with the upper part of the side wall of the second rectifying tower, and the fourth return pipe is provided with an eighth valve.
And a ninth valve is arranged on the third pipeline.
And a seventh valve is arranged on the third pipeline.
Adopt above-mentioned technical scheme to have following beneficial effect:
the utility model separates the material obtained by benzene hydrogenation through the benzene separation tower, the component obtained at the tower bottom of the benzene separation tower is high boiling point component benzene with the purity more than 99.5 percent, can be directly used as raw material to synthesize cyclohexanol, the distilled components of benzene separation tower mainly comprise cyclohexene, cyclohexane, small amount of benzene, and byproduct impurities such as methylcyclopentane, hexane, and pentane, the fractions enter a cyclohexene separating tower, cyclohexene with the purity of more than 99.5 percent is obtained at the tower bottom of the cyclohexene separating tower, the target product cyclohexanol can be obtained by directly hydrating the raw material, the crude cyclohexane (the main component is cyclohexane, and the crude cyclohexane contains a small amount of benzene, cyclohexene and byproduct impurities) is obtained from the top of the cyclohexene separation tower, and the benzene and the cyclohexene in the crude cyclohexane are hydrogenated and reduced into cyclohexane through a hydrogenation device, so that the impurities benzene and cyclohexene can be effectively recycled, and the utilization rate of the raw material is improved. The method comprises the steps of (1) passing a material (the main component of which is cyclohexane and byproduct impurities such as methylcyclopentane, hexane and pentane) subjected to hydrogenation reduction through a first rectifying tower, distilling light components (the main component of which is the impurities and a small amount of cyclohexane) in the material, discharging the light components to a second rectifying tower for further rectification, discharging the light components to a cyclohexane tank of which the purity is more than 99.9% to serve as a raw material for standby, performing secondary rectification on the light components in the second rectifying tower, wherein the light components are mostly impurities, the content of the cyclohexane is lower than 5%, distilling the light components to the light component tank, and directly selling the light components as light oil, so that the utilization rate of the byproduct impurities can be effectively improved, and the income of enterprises can be further improved. The component obtained from the tower bottom of the second rectifying tower is cyclohexane with the purity of more than 99.9 percent, and the cyclohexane is discharged to a cyclohexane tank to be used as a raw material for later use. The utility model discloses to utilize benzene to separate through benzene separation, cyclohexene separation, hydrogenation, second grade rectification as each component of initial raw materials preparation cyclohexanol technology raw materials, not only effectively separated benzene wherein and returned as raw materials use, cyclohexene is as raw materials synthesis cyclohexanol, has still recycled benzene and cyclohexene that mix with, has improved the output of cyclohexane, and has effectively utilized the by-product impurity, realizes the make full use of material.
The following further description is made with reference to the accompanying drawings and detailed description.
Drawings
Fig. 1 is a schematic connection diagram of the present invention.
In the drawing, 1 is a benzene separation column, 11 is a first condenser, 12 is a first buffer tank, 13 is a first feed pump, 14 is a first return pipe, 2 is a cyclohexene separation column, 21 is a second condenser, 22 is a second buffer tank, 23 is a second feed pump, 24 is a second return pipe, 3 is a hydrogenation apparatus, 4 is a first rectification column, 41 is a third condenser, 42 is a third buffer tank, 43 is a third feed pump, 44 is a third return pipe, 5 is a second rectification column, 51 is a fourth condenser, 52 is a fourth buffer tank, 53 is a fourth feed pump, 54 is a fourth return pipe, 6 is a benzene tank, 7 is a cyclohexene tank, 8 is a cyclohexane tank, 9 is a light component tank, 101 is a first pipeline, 102 is a second pipeline, 103 is a third pipeline, 104 is a fourth pipeline, 105 is a fifth pipeline, a is a first valve, b is a second valve, c is a third valve, d is a fourth valve, e is the fifth valve, f is the sixth valve, g is the seventh valve, h is the eighth valve, i is the ninth valve.
Detailed Description
The utility model discloses in, do not mark the device, the equipment of specific structure, adopt the conventional device or the equipment in chemical industry field usually, do not mark the installation, the connected mode that adopt the conventional installation in chemical industry field usually of specific installation, connected mode or install, connect according to the guide suggestion of producer.
Referring to fig. 1, a specific embodiment of a cyclohexanol process feedstock separation and recovery system is shown. The separation and recovery system for the cyclohexanol process raw material comprises a benzene separation tower 1, a cyclohexene separation tower 2, a hydrogenation device 3, a first rectifying tower 4 and a second rectifying tower 5. The feed inlet of the benzene separation tower 1 is used for being connected with a benzene hydrogenation device, a material obtained by hydrogenating a benzene raw material enters the benzene hydrogenation device, a discharge outlet at the top of the benzene separation tower 1 passes through a first condenser 11 and a first buffer tank 12 and supplies a material to the cyclohexene separation tower 2 through a first pipeline 101, and a discharge outlet at the bottom of the benzene separation tower 1 supplies a material to the benzene tank 6 through a first pipeline 101. in this embodiment, the first pipeline 101 is provided with a first material conveying pump 13 and a first valve a, the first valve a is positioned at the downstream of the first material conveying pump 13, specifically, the device further comprises a first return pipe 14, the upstream end of the first return pipe 14 is connected with the first pipeline 101 and positioned between the first material conveying pump 13 and the first valve a, the downstream end is connected with the upper part of the side wall of the benzene separation tower 1, the first return pipe 14 is provided with a second valve b, and part of condensate is returned to the benzene separation tower by controlling the first valve and the second, the distillation amount of benzene is reduced. The top discharge port of the cyclohexene separating tower 2 supplies the hydrogenation device 3 through the second pipeline 102 via the second condenser 21 and the second buffer tank 22, and the bottom discharge port of the cyclohexene separating tower 2 supplies the cyclohexene tank 7, in this embodiment, the second pipeline 102 is provided with the second material delivery pump 23 and the third valve c, the third valve c is located at the downstream of the second material delivery pump 23, specifically, the device further comprises the second return pipe 24, the upstream end of the second return pipe 24 is connected with the second pipeline 102 and located between the second material delivery pump 23 and the third valve c, the downstream end is connected with the upper portion of the side wall of the cyclohexene separating tower 2, the second return pipe 24 is provided with the fourth valve d, and by controlling the third valve and the fourth valve, part of the condensate flows back to the cyclohexene separating tower, so that the distillation amount of cyclohexene is reduced. The discharge port of the hydrogenation apparatus 3 supplies the first rectifying column 4 through a third pipeline 103, and specifically, the third pipeline 103 is provided with a ninth valve i. The top discharge port of the first rectifying tower 4 supplies material to the second rectifying tower 5 through a fourth pipeline 104 by a third condenser 41 and a third buffer tank 42, and the bottom discharge port of the first rectifying tower 4 supplies material to the cyclohexane tank 8, in this embodiment, a third material conveying pump 43 and a fifth valve e are arranged on the fourth pipeline 104, the fifth valve e is located at the downstream of the third material conveying pump 43, specifically, the third reflux pipe 44 is further included, the upstream end of the third reflux pipe 44 is connected with the fourth pipeline 104 and located between the third material conveying pump 43 and the fifth valve e, the downstream end is connected with the upper part of the side wall of the first rectifying tower 4, and a sixth valve f is arranged on the third reflux pipe 44, so that part of condensate flows back to the first rectifying tower by controlling the fifth valve and the sixth valve, and the distillation amount of cyclohexane is reduced. The top discharge port of the second rectifying tower 5 supplies the light component tank 9 through a fifth pipeline 105 through a fourth condenser 51 and a fourth buffer tank 52, and the bottom discharge port of the second rectifying tower 5 supplies the cyclohexane tank 8, in this embodiment, a fourth material delivery pump 53 and a seventh valve g are arranged on the fifth pipeline 105, the seventh valve g is located at the downstream of the fourth material delivery pump 53, specifically, the fourth reflux pipe 54 is further included, the upstream end of the fourth reflux pipe 54 is connected with the fifth pipeline 105, is located between the fourth material delivery pump 53 and the seventh valve g, the downstream end is connected with the upper part of the side wall of the second rectifying tower 5, an eighth valve h is arranged on the fourth reflux pipe 54, and by controlling the seventh valve and the eighth valve, part of condensate is controlled to reflux to the second rectifying tower, and the distillation amount of cyclohexane is reduced.
The utility model discloses an operating principle does, and benzene is as initial raw materials, through the hydrogenation after, obtains the material and contains unreacted benzene, the cyclohexene that the hydrogenation obtained to and the cyclohexane that excessive hydrogenation obtained, methylcyclopentane, hexane, pentane that the byproduct obtained. The components enter a benzene separation tower, after separation, the high boiling point component benzene with the purity of more than 99.5 percent is obtained at the bottom of the benzene separation tower and is returned to be continuously used as an initial raw material, the distilled components of the benzene separation tower mainly comprise cyclohexene, cyclohexane, a small amount of benzene and byproduct impurities, the fractions enter the cyclohexene separation tower, the cyclohexene with the purity of more than 99.5 percent is obtained at the bottom of the cyclohexene separation tower and is directly used as a raw material to hydrate to obtain a target product cyclohexanol, the crude cyclohexane (the main component is cyclohexane, the crude cyclohexane contains a small amount of benzene, cyclohexene and byproduct impurities) is obtained at the top of the cyclohexene separation tower, the benzene and the cyclohexene which are included in the crude cyclohexane are hydrogenated and reduced into cyclohexane through a hydrogenation device, the materials (the main component is cyclohexane and the byproduct impurities) which are hydrogenated and reduced pass through a first rectifying tower, and light components (the main component is the impurities and the, discharging to a second rectifying tower for further rectification, discharging the components obtained at the tower bottom of the first rectifying tower to a cyclohexane tank as raw materials for later use, performing secondary rectification on light components in the second rectifying tower, wherein most of the light components are impurities, the content of the cyclohexane is lower than 5%, distilling to the light component tank, directly selling the light components as light oil, discharging the components obtained at the tower bottom of the second rectifying tower to the cyclohexane tank as raw materials for later use, and discharging the components obtained at the tower bottom of the first rectifying tower to the cyclohexane tank as raw materials for later use.
Claims (10)
1. A separation recovery system of cyclohexanol technology raw materials which characterized in that: comprises a benzene separation tower (1), a cyclohexene separation tower (2), a hydrogenation device (3), a first rectifying tower (4) and a second rectifying tower (5),
the feed inlet of the benzene separation tower (1) is used for being connected with a benzene hydrogenation device, the discharge outlet at the top of the benzene separation tower (1) supplies materials to the cyclohexene separation tower (2) through a first pipeline (101) through a first condenser (11) and a first buffer tank (12), the discharge outlet at the bottom of the benzene separation tower (1) supplies materials to the benzene tank (6),
the tower top discharge opening of the cyclohexene separating tower (2) is used for feeding a hydrogenation device (3) through a second pipeline (102) through a second condenser (21) and a second buffer tank (22), the tower bottom discharge opening of the cyclohexene separating tower (2) is used for feeding a cyclohexene tank (7), the discharge opening of the hydrogenation device (3) is used for feeding a first rectifying tower (4) through a third pipeline (103), the tower top discharge opening of the first rectifying tower (4) is used for feeding a second rectifying tower (5) through a fourth pipeline (104) through a third condenser (41) and a third buffer tank (42), and the tower bottom discharge opening of the first rectifying tower (4) is used for feeding a cyclohexane tank (8),
the top discharge port of the second rectifying tower (5) supplies the light component tank (9) through a fifth pipeline (105) through a fourth condenser (51) and a fourth buffer tank (52), and the bottom discharge port of the second rectifying tower (5) supplies the cyclohexane tank (8).
2. The system for separating and recovering cyclohexanol process material as recited in claim 1, wherein: the first pipeline (101) is provided with a first material conveying pump (13) and a first valve (a), and the first valve (a) is positioned at the downstream of the first material conveying pump (13).
3. The system for separating and recovering cyclohexanol process material as recited in claim 2, wherein: the benzene separation tower is characterized by further comprising a first return pipe (14), the upstream end of the first return pipe (14) is connected with the first pipeline (101) and located between the first material conveying pump (13) and the first valve (a), the downstream end of the first return pipe is connected with the upper portion of the side wall of the benzene separation tower (1), and the first return pipe (14) is provided with a second valve (b).
4. The system for separating and recovering cyclohexanol process material as recited in claim 1, wherein: and a second material conveying pump (23) and a third valve (c) are arranged on the second pipeline (102), and the third valve (c) is positioned at the downstream of the second material conveying pump (23).
5. A separation and recovery system for cyclohexanol process material as recited in claim 4, wherein: the device is characterized by further comprising a second return pipe (24), wherein the upstream end of the second return pipe (24) is connected with the second pipeline (102) and is positioned between the second material conveying pump (23) and the third valve (c), the downstream end of the second return pipe is connected with the upper portion of the side wall of the cyclohexene separating tower (2), and the second return pipe (24) is provided with a fourth valve (d).
6. The system for separating and recovering cyclohexanol process material as recited in claim 1, wherein: and a third material conveying pump (43) and a fifth valve (e) are arranged on the fourth pipeline (104), and the fifth valve (e) is positioned at the downstream of the third material conveying pump (43).
7. The system for separating and recovering cyclohexanol process material as recited in claim 6, wherein: the rectifying tower further comprises a third return pipe (44), the upstream end of the third return pipe (44) is connected with a fourth pipeline (104) and located between a third material conveying pump (43) and a fifth valve (e), the downstream end of the third return pipe is connected with the upper portion of the side wall of the first rectifying tower (4), and a sixth valve (f) is arranged on the third return pipe (44).
8. The system for separating and recovering cyclohexanol process material as recited in claim 1, wherein: and a fourth material conveying pump (53) and a seventh valve (g) are arranged on the fifth pipeline (105), and the seventh valve (g) is positioned at the downstream of the fourth material conveying pump (53).
9. A system for the separation and recovery of cyclohexanol process material as recited in claim 8, wherein: the rectifying tower further comprises a fourth return pipe (54), the upstream end of the fourth return pipe (54) is connected with a fifth pipeline (105) and is located between the fourth material conveying pump (53) and the seventh valve (g), the downstream end of the fourth return pipe is connected with the upper portion of the side wall of the second rectifying tower (5), and an eighth valve (h) is arranged on the fourth return pipe (54).
10. The system for separating and recovering cyclohexanol process material as recited in claim 1, wherein: and a ninth valve (i) is arranged on the third pipeline (103).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022158483.1U CN213506663U (en) | 2020-09-27 | 2020-09-27 | Separation recovery system of cyclohexanol technology raw materials |
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| CN202022158483.1U CN213506663U (en) | 2020-09-27 | 2020-09-27 | Separation recovery system of cyclohexanol technology raw materials |
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| CN202022158483.1U Active CN213506663U (en) | 2020-09-27 | 2020-09-27 | Separation recovery system of cyclohexanol technology raw materials |
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