CN212476585U - Waste heat recovery system of rectifying unit in cyclohexanol production process - Google Patents
Waste heat recovery system of rectifying unit in cyclohexanol production process Download PDFInfo
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- CN212476585U CN212476585U CN202020483363.6U CN202020483363U CN212476585U CN 212476585 U CN212476585 U CN 212476585U CN 202020483363 U CN202020483363 U CN 202020483363U CN 212476585 U CN212476585 U CN 212476585U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model provides a rectification unit waste heat recovery system in cyclohexanol production process, it includes the benzene knockout tower, the cyclohexene knockout tower, cyclohexene knockout tower and extractant storage tank and circulating pump, add benzene knockout tower second reboiler and cyclohexene knockout tower second reboiler respectively through the tower cauldron at benzene knockout tower and cyclohexene knockout tower, the heat of reaction feed liquid is recycled through the recovery in the system of will separating purification, make full use of benzene knockout tower and cyclohexene knockout tower cauldron liquid waste heat heats benzene knockout tower second reboiler and cyclohexene knockout tower second reboiler respectively. The utility model discloses a waste heat recovery system can save tower cauldron high-temperature steam's consumption, and can make benzene recovery tower and cyclohexene recovery tower cauldron extractant temperature reduce, reducible cooling water use amount simultaneously to can practice thrift the energy consumption, reduction in production cost, thereby have better result of use.
Description
Technical Field
The utility model relates to a cyclohexanol preparation equipment technical field, in particular to rectification unit waste heat recovery system in cyclohexanol production process.
Background
Cyclohexanol is an important chemical intermediate and solvent, is mainly used for producing products such as nylon 6, nylon 66 and the like, and the route for industrially producing cyclohexanol mainly comprises the following steps: (1) hydrogenation of benzene to prepare cyclohexane, and partial oxidation of the cyclohexane by reaction with oxygen in the air to prepare cyclohexanol; (2) hydrogenating phenol to produce cyclohexanol. The preparation source of the phenol is more complex and the price is more expensive than that of the benzene, so the application of the phenol hydrogenation process is limited to a certain extent; (3) partial hydrogenation of benzene is carried out to produce cyclohexene, and then the cyclohexene is subjected to hydration reaction under the catalysis of acid to obtain cyclohexanol. Wherein, the process route for preparing cyclohexanol by cyclohexene produced by partial hydrogenation of benzene is as follows: the method comprises the steps of reacting raw material benzene and hydrogen in a reaction kettle under the action of a ruthenium catalyst to generate a product cyclohexene and a byproduct cyclohexane, then separating unreacted raw material benzene, the product cyclohexene, the byproduct cyclohexane and the like in a reaction mixture through a series of extractive distillation technologies, and conveying the obtained pure cyclohexene to a hydration reactor to prepare cyclohexanol.
Theoretically, compared with the traditional cyclohexane oxidation route, the partial hydrogenation route of benzene saves one third of hydrogen, and has the advantages of low process energy consumption, fewer byproducts, high production safety and the like. However, the temperature required by each rectifying unit in the separation process of the benzene partial hydrogenation product is different, and the heat of each rectifying tower is not reasonably redistributed and utilized in the traditional separation and purification process, so that the energy waste is caused, and the production cost is increased. Meanwhile, in the production process of cyclohexanol, reboilers of the benzene hydrogenation product extraction rectifying tower adopt a medium-pressure steam heating mode, a large amount of high-temperature steam is consumed, the problem of high production energy consumption is caused, and the energy utilization is unreasonable.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model aims at providing a rectification unit waste heat recovery system in cyclohexanol production process to but the waste heat of the tower bottom liquid of make full use of benzene recovery tower and cyclohexene recovery tower, thereby can practice thrift the use amount of steam consumption and cooling water, realize reducing the production energy consumption and reduce the wasting of resources.
In order to achieve the above purpose, the technical scheme of the utility model is realized like this:
a waste heat recovery system of a rectification unit in a cyclohexanol production process comprises a benzene separation tower, a benzene recovery tower, a cyclohexene separation tower, a cyclohexene recovery tower, an extractant storage tank and a circulating pump;
an inlet of the benzene separation tower is connected with the extractant storage tank and an external reaction device filled with benzene, cyclohexane and cyclohexene, an outlet at the upper end of the benzene separation tower is connected with an inlet of the cyclohexene separation tower, an outlet at the lower end of the benzene separation tower is connected with an inlet of the benzene recovery tower, a first reboiler of the benzene separation tower and a second reboiler of the benzene separation tower are arranged on the benzene separation tower in parallel, an inlet of the second reboiler of the benzene separation tower is connected with an outlet at the lower end of the benzene recovery tower, and an outlet of the second reboiler of the benzene separation tower is connected with an inlet of the extractant storage tank;
the import of cyclohexene knockout tower with the extractant storage tank links to each other, just the lower extreme export of cyclohexene knockout tower with the import of cyclohexene recovery tower links to each other, in the last parallelly connected first reboiler of cyclohexene knockout tower and the cyclohexene knockout tower second reboiler that is equipped with of cyclohexene knockout tower, the import of cyclohexene knockout tower second reboiler with the lower extreme export of cyclohexene recovery tower links to each other, the export of cyclohexene knockout tower second reboiler through the circulating pump with the import of extractant storage tank links to each other.
Further, an outlet at the upper end of the benzene recovery tower is connected with an external benzene storage tank.
Furthermore, an outlet at the upper end of the cyclohexene separation tower is connected with a process treatment device in the next process.
Furthermore, a circulating pump is arranged on a pipeline connecting an outlet at the lower end of the benzene separation tower with an inlet of the benzene recovery tower.
Furthermore, a circulating pump is arranged on a pipeline connecting an outlet at the lower end of the cyclohexene separation tower and an inlet of the cyclohexene recovery tower.
Further, the pressure drop of the benzene separation tower and the pressure drop of the cyclohexene separation tower are both 0.01-0.04MPa, and the reflux ratio of the benzene separation tower to the reflux ratio of the cyclohexene separation tower are both greater than 0.8.
Compared with the prior art, the utility model discloses following advantage has:
rectification unit waste heat recovery system in cyclohexanol production process, add benzene knockout tower second reboiler and cyclohexene knockout tower second reboiler respectively through the tower cauldron at benzene knockout tower and cyclohexene knockout tower, the heat of reaction feed liquid recycles through retrieving in the separation and purification system, make full use of benzene knockout tower and cyclohexene knockout tower cauldron liquid waste heat respectively to benzene knockout tower second reboiler and cyclohexene knockout tower second reboiler, thereby can save tower cauldron high temperature steam's consumption, and can make benzene knockout tower and cyclohexene knockout tower cauldron extractant temperature reduce, reducible cooling water use amount simultaneously, and can practice thrift the energy consumption, reduction in production cost.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without undue limitation. In the drawings:
fig. 1 is a schematic structural diagram of a waste heat recovery system of a rectification unit in a cyclohexanol production process according to an embodiment of the present invention;
description of reference numerals:
1-benzene separation tower, 2-benzene recovery tower, 3-cyclohexene separation tower and 4-cyclohexene recovery tower;
10-an extractant storage tank, 11-a first reboiler of a benzene separation tower, 12-a second reboiler of the benzene separation tower, 21-a reboiler of a benzene recovery tower, 31-a first reboiler of a cyclohexene separation tower, 32-a second reboiler of the cyclohexene separation tower, 41-a reboiler of the cyclohexene recovery tower, and 20-a circulating pump.
Detailed Description
It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it should be noted that the terms "upper", "lower", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, which are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first" and "second" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
The embodiment relates to a rectification unit waste heat recovery system in cyclohexanol production process, an exemplary structure thereof is shown in fig. 1, this waste heat recovery system includes benzene knockout tower 1, benzene knockout tower 2, cyclohexene knockout tower 3, cyclohexene knockout tower 4 and extractant storage tank 10 and circulating pump 20, through add benzene knockout tower second reboiler 12 and cyclohexene knockout tower second reboiler 32 respectively in the tower cauldron of benzene knockout tower 1 and cyclohexene knockout tower 3, the heat of reaction feed liquid in the separation purification system is recycled through retrieving, make full use of benzene knockout tower 2 and cyclohexene knockout tower 4 tower bottom liquid waste heat respectively heats benzene knockout tower second reboiler 12 and cyclohexene knockout tower second reboiler 32.
Specifically, as shown in fig. 1, an inlet of the benzene separation tower 1 of the present embodiment is connected to an extractant storage tank 10 and an external reaction device containing benzene, cyclohexane, and cyclohexene through a pipeline, an outlet at an upper end of the benzene separation tower 1 is connected to an inlet of the cyclohexene separation tower 3 through a pipeline, an outlet at a lower end of the benzene separation tower 1 is connected to an inlet of the benzene recovery tower 2 through a pipeline, and a first reboiler 11 of the benzene separation tower and a second reboiler 12 of the benzene separation tower are installed in parallel on the benzene separation tower 1. Wherein, the import of benzene knockout tower second reboiler 12 passes through the pipeline with the lower extreme export of benzene knockout tower 2 and links to each other, and the export of benzene knockout tower second reboiler 12 passes through the pipeline with the import of extractant storage tank 10 and links to each other, promptly, regards the tower bottom output of benzene knockout tower 2 as the heat source of benzene knockout tower second reboiler 12 to the tower bottom of benzene knockout tower 1 heats.
An inlet of the cyclohexene separating tower 3 is connected with the extractant storage tank 10 through a pipeline, an outlet at the lower end of the cyclohexene separating tower 3 is connected with an inlet of the cyclohexene recovery tower 4 through a pipeline, and a first reboiler 31 of the cyclohexene separating tower and a second reboiler 32 of the cyclohexene separating tower are installed on the cyclohexene separating tower 3 in parallel. Wherein, the inlet of the second reboiler 32 of the cyclohexene separating column is connected with the outlet at the lower end of the cyclohexene recovery column 4 through a pipeline, and the outlet of the second reboiler 32 of the cyclohexene separating column is connected with the inlet of the extractant storage tank 10 through a pipeline by a circulating pump 20. That is, the high-temperature extractant in the bottom of the cyclohexene recovery column 4 is used as the heat source of the second reboiler 32 in the cyclohexene separation column to heat the bottom liquid in the cyclohexene separation column 3.
In addition, an outlet at the upper end of the benzene recovery tower 2 is connected with an external benzene storage tank, so that the benzene distilled from the top of the benzene recovery tower 2 can be recovered and reused. An outlet at the upper end of the cyclohexene separation tower 3 is connected with a process treatment device in the next process, so that the process treatment of the next process can be carried out on the overhead distillate of the cyclohexene separation tower 3, wherein the overhead distillate of the cyclohexene separation tower 3 comprises cyclohexane, cyclohexene, a small amount of benzene and an extracting agent. In order to facilitate the transportation of the tower bottoms, in this embodiment, a circulating pump 20 is disposed on a pipeline connecting the outlet at the lower end of the benzene separation tower 1 and the inlet of the benzene recovery tower 2. Similarly, a circulating pump 20 is arranged on a pipeline connecting the outlet at the lower end of the cyclohexene separation tower 3 and the inlet of the cyclohexene recovery tower 4.
In this embodiment, the pressure drop of the benzene separation tower 1 and the pressure drop of the cyclohexene separation tower 3 are both 0.01-0.04MPa, and the reflux ratio of the benzene separation tower 1 and the reflux ratio of the cyclohexene separation tower 3 are both greater than 0.8. Note that, in the present example, the benzene recovery column 2 is provided with a benzene recovery column reboiler 21, and similarly, the cyclohexene recovery column 4 is also provided with a cyclohexene recovery column reboiler 41.
In the production process of cyclohexanol, benzene is partially hydrogenated to produce cyclohexene, and after the reaction is completed, unreacted benzene and cyclohexane as a byproduct exist in the product and need to be further separated and purified. The separation step comprises: sending a mixture of benzene, cyclohexane and cyclohexene obtained after partial hydrogenation reaction of benzene and an extracting agent from an extracting agent tank into a benzene separation tower 1 through a pipeline, extracting benzene and the extracting agent from the bottom of the benzene separation tower 1, and then conveying the benzene and the extracting agent into a benzene recovery tower 2 for rectification; pure benzene is distilled from the top of the benzene recovery tower 2 and is sent back to the benzene storage tank as a raw material for recycling, the extractant is discharged from the tower kettle, the temperature of the extractant is higher at the moment and a large amount of waste heat is generated, so the extractant in the tower kettle of the benzene recovery tower 2 is conveyed to a second reboiler 12 of the benzene separation tower to heat the tower kettle liquid of the benzene separation tower 1, and the extractant after heat exchange is returned to the extractant storage tank 10 for recycling.
Cyclohexane, cyclohexene, a small amount of benzene and an extracting agent are discharged from the top of the benzene separation tower 1 and are conveyed to a cyclohexene separation tower 3. Wherein, a mixture comprising cyclohexane, a small amount of benzene, cyclohexene and an extracting agent is discharged from the top of the cyclohexene separation column 3, and then the mixture is conveyed to the next process for refining. And the cyclohexene and the extractant are discharged from the bottom of the cyclohexene separating tower 3 and are conveyed to a cyclohexene recovery tower 4, pure cyclohexene is distilled from the top of the cyclohexene recovery tower 4, the extractant is discharged from the bottom of the cyclohexene recovery tower 4, and the extractant at the position is conveyed to a second reboiler 32 of the cyclohexene separating tower due to the fact that the extractant has high temperature, so that the tower bottom liquid of the cyclohexene separating tower 3 is heated, and the extractant after heat exchange is finished is returned to an extractant storage tank 10 for recycling.
The utility model discloses a waste heat recovery system during operation, come from reaction system's benzene, cyclohexane, cyclohexene and come from the extractant of extractant storage tank 10 add benzene knockout tower 1 in, wherein, the tower cauldron temperature of benzene knockout tower 1 is 124.7 ℃, the top of the tower mole reflux ratio is greater than 0.8, the pressure drop of whole tower is 0.01-0.04MPa, through the extractive distillation process at the separation of the tower bottom of benzene knockout tower 1 obtain benzene and extractant, pass through pipeline and circulating pump 20 with the distillate of the tower bottom and carry in benzene knockout tower 2, in order to carry out further separation. It should be noted that the overhead molar reflux ratio of the benzene recovery column 2 is more than 0.8, and the pressure drop of the whole column is 0.01-0.04 MPa.
Pure benzene is distilled from the top of the benzene recovery tower 2 and is conveyed back to the benzene storage tank to be used as a raw material for continuous use, an extracting agent is distilled from the bottom of the benzene recovery tower 2, the temperature of the extracting agent is higher than 148.8 ℃, a large amount of waste heat is carried, if the extracting agent is continuously recycled, cooling treatment needs to be carried out firstly, but a large amount of cooling water is consumed during cooling, and electric power is consumed, so that the waste heat carried by the extracting agent is conveyed into a second reboiler 12 of the benzene separation tower through a pipeline to heat the tower bottom liquid of the benzene separation tower 1, the temperature of the extracting agent after heat exchange is 129.7-136.3 ℃, and finally the extracting agent is conveyed back to the extracting agent storage tank 10 through a circulating pump 20, so that the use amount of the cooling water is reduced, and the use amount of steam reboiling of the tower bottom of the benzene separation tower.
Cyclohexane, cyclohexene, a small amount of benzene and an extracting agent are obtained at the top of a benzene separating tower 1, the overhead distillate and the extracting agent from an extracting agent storage tank 10 are conveyed to a cyclohexene separating tower 3 through a pipeline, wherein the overhead molar reflux ratio of the cyclohexene separating tower 3 is greater than 0.8, the pressure drop of the whole tower is 0.01-0.04MPa, the kettle temperature of the cyclohexene separating tower 3 is 122.2 ℃, a mixture of the cyclohexane, the small amount of benzene, the cyclohexene and the extracting agent is distilled off at the top of the tower, and then the distilled mixture is subjected to the process treatment of the next procedure. And the mixed liquid of the cyclohexene and the extracting agent obtained from the bottom of the cyclohexene separating tower 3 is conveyed into a cyclohexene recovery tower 4 through a pipeline and a circulating pump 20, and is continuously separated and refined.
It should be noted that the overhead molar reflux ratio of the cyclohexene recovery tower 4 is greater than 0.8, the pressure drop of the whole tower is 0.01-0.04MPa, the high-purity cyclohexene product is obtained at the overhead of the cyclohexene recovery tower 4, the extractant distilled from the bottom of the cyclohexene recovery tower 4, the temperature of the extractant at the position of 153 ℃, which also contains a large amount of waste heat, is conveyed to the second reboiler 32 of the cyclohexene separation tower through a pipeline to heat the bottom liquid of the cyclohexene separation tower 3, the temperature of the extractant after heat exchange is 132-141.0 ℃, and is conveyed back to the extractant storage tank 10 through the circulating pump 20, so that the usage amount of high-temperature steam can be saved, the energy can be comprehensively utilized, and the cost can be saved.
The above description is only for the preferred embodiment of the present invention, and is not intended to limit the present invention, and any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (6)
1. A rectification unit waste heat recovery system in cyclohexanol production process is characterized by comprising a benzene separation tower (1), a benzene recovery tower (2), a cyclohexene separation tower (3), a cyclohexene recovery tower (4), an extractant storage tank (10) and a circulating pump (20);
an inlet of the benzene separation tower (1) is connected with the extractant storage tank (10) and an external reaction device filled with benzene, cyclohexane and cyclohexene, an outlet at the upper end of the benzene separation tower (1) is connected with an inlet of the cyclohexene separation tower (3), an outlet at the lower end of the benzene separation tower (1) is connected with an inlet of the benzene recovery tower (2), a first reboiler (11) of the benzene separation tower and a second reboiler (12) of the benzene separation tower are arranged on the benzene separation tower (1) in parallel, an inlet of the second reboiler (12) of the benzene separation tower is connected with an outlet at the lower end of the benzene recovery tower (2), and an outlet of the second reboiler (12) of the benzene separation tower is connected with an inlet of the extractant storage tank (10);
the import of cyclohexene knockout tower (3) with extractant storage tank (10) links to each other, just the lower extreme export of cyclohexene knockout tower (3) with the import of cyclohexene recovery tower (4) links to each other, in the parallel first reboiler (31) of cyclohexene knockout tower and cyclohexene knockout tower second reboiler (32) of being equipped with on cyclohexene knockout tower (3), the import of cyclohexene knockout tower second reboiler (32) with the lower extreme export of cyclohexene recovery tower (4) links to each other, the export of cyclohexene knockout tower second reboiler (32) through circulating pump (20) with the import of extractant storage tank (10) links to each other.
2. The system for recovering the waste heat of the rectifying unit in the production process of cyclohexanol as recited in claim 1, wherein: and an outlet at the upper end of the benzene recovery tower (2) is connected with an external benzene storage tank.
3. The system for recovering the waste heat of the rectifying unit in the production process of cyclohexanol as recited in claim 1, wherein: and an upper end outlet of the cyclohexene separating tower (3) is connected with a process treatment device of the next process.
4. The system for recovering the waste heat of the rectifying unit in the production process of cyclohexanol as recited in claim 1, wherein: and a circulating pump (20) is arranged on a pipeline connecting the outlet at the lower end of the benzene separation tower (1) and the inlet of the benzene recovery tower (2).
5. The system for recovering the waste heat of the rectifying unit in the production process of cyclohexanol as recited in claim 1, wherein: and a circulating pump (20) is arranged on a pipeline connecting the outlet at the lower end of the cyclohexene separating tower (3) and the inlet of the cyclohexene recovery tower (4).
6. The system for recovering the waste heat of the rectifying unit in the production process of cyclohexanol as recited in claim 1, wherein: the pressure drop of the benzene separation tower (1) and the pressure drop of the cyclohexene separation tower (3) are both 0.01-0.04MPa, and the reflux ratio of the benzene separation tower (1) and the reflux ratio of the cyclohexene separation tower (3) are both greater than 0.8.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113651672A (en) * | 2021-08-05 | 2021-11-16 | 杭州浥能科技有限公司 | Method for separating cyclohexene |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113651672A (en) * | 2021-08-05 | 2021-11-16 | 杭州浥能科技有限公司 | Method for separating cyclohexene |
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