CN213623926U - Device for producing normal hexane and isohexane - Google Patents
Device for producing normal hexane and isohexane Download PDFInfo
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- CN213623926U CN213623926U CN202022459941.5U CN202022459941U CN213623926U CN 213623926 U CN213623926 U CN 213623926U CN 202022459941 U CN202022459941 U CN 202022459941U CN 213623926 U CN213623926 U CN 213623926U
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Abstract
A device for producing normal hexane and isohexane comprises a raw material product heat exchanger, a heater, a hydrogenation reactor, a recycle hydrogen desulfurization reactor, a reaction product cooler, a low-pressure separator, a recycle hydrogen separation tank, a recycle hydrogen compressor, a light component removal tower and a normal hexane removal tower; oil at an oil outlet of the low-pressure separator enters a fractionation system, and the fractionation system comprises a light component removal tower and a normal hexane removal tower; the oil outlet of the low-pressure separator is connected with the feed inlet of the light component removal tower, and the top of the light component removal tower is connected with a petroleum ether I outlet device through a pipeline; a side line extraction port of the light component removal tower is connected with a feed inlet of the n-hexane removal tower, and a bottom oil outlet of the light component removal tower is connected with a petroleum ether III outlet device through a pipeline; the top of the normal hexane removal tower is connected with an isohexane outlet device pipeline, and the bottom of the normal hexane removal tower is connected with a normal hexane outlet device pipeline; the dehydrogenation component tower is a clapboard tower. The method has the advantages that one partition plate tower replaces two towers, and the raw materials are processed into products with different brands by using simple fractionation equipment.
Description
Technical Field
The utility model belongs to the technical field of petrochemical, specificly relate to a device of production n-hexane, isohexane.
Background
In recent years, with the increasing pressure of resource shortage, environmental protection and carbon emission reduction, reducing energy consumption and carbon emission by using an advanced process enhancement technology has become an industrial research hotspot. In foreign countries, the technology of the clapboard tower is mainly applied to the field of olefin production, and the research on the field is later in China, so that the technology is just started in recent years and has little application in industry.
N-hexane is one of the most industrially used hydrocarbon solvents, and is the most representative nonpolar solvent. N-hexane is used as an important chemical raw material and a solvent, has been widely used in the industries of medicine, chemical industry, high molecular materials, rubber industry, food analysis and the like, and can be used as a diluent of essential oil, a coolant in caprolactam production, a vegetable oil extracting agent in food production and the like. Isohexane has low boiling point, easy removal, good safety and low energy cost, has very wide prospect in the fields of aerosol product production and precise instruments, and the preparation technology of isohexane has become the focus of attention of researchers.
In industrial production, the production of normal hexane and isohexane usually requires pretreatment of production raw materials, and then a series of technological processes such as double-tower continuous rectification are carried out to finally obtain qualified hexane oil products. With the increasingly strict requirements on the deterioration and environmental protection of crude oil, the utilization of high-tech means to improve the production efficiency, save energy and reduce emission, and the production of high-quality products becomes the main direction of research at present.
SUMMERY OF THE UTILITY MODEL
The utility model provides an introduce baffle tower, a tower and replace two towers, the device of production normal hexane, isohexane of different trade marks product is processed into with the raw materials to fractionation equipment simple to use.
In order to realize the purpose of the utility model, the utility model adopts the following technical scheme: a device for producing normal hexane and isohexane comprises a raw material product heat exchanger, a heater, a hydrogenation reactor, a recycle hydrogen desulfurization reactor, a reaction product cooler, a low-pressure separator, a recycle hydrogen separation tank, a recycle hydrogen compressor, a light component removal tower and a normal hexane removal tower;
a raw material inlet of the raw material product heat exchanger is connected with an outlet of a raw material pump (the raw material pump is arranged on a conveying pipeline of a medium raw material and used for providing power for raw material operation, is a more conventional arrangement in the industry and is prevented from being shown in the figure) through a pipeline, and a raw material outlet of the raw material product heat exchanger is connected with a feed inlet of a heater through a pipeline; the discharge hole of the heater is connected with the feed inlet of the hydrogenation reactor through a pipeline, the discharge hole of the hydrogenation reactor is connected with the product feed inlet of the raw material product heat exchanger through a pipeline, the product discharge hole of the raw material product heat exchanger is connected with the feed inlet of the reaction product cooler through a pipeline, and the discharge hole of the reaction product cooler is connected with the feed inlet of the low-pressure separator through a pipeline;
the gas outlet of the low-pressure separator is connected with the gas inlet of the circulating hydrogen separation tank, the gas outlet of the circulating hydrogen separation tank is connected with the gas inlet of the circulating hydrogen compressor, the fresh hydrogen inlet (the fresh hydrogen is supplemented from the outside) is connected with the gas outlet pipeline of the circulating hydrogen compressor, the gas outlet of the circulating hydrogen compressor is connected with the inlet of the circulating hydrogen desulfurization reactor, and the outlet of the circulating hydrogen desulfurization reactor is connected with the outlet pipeline of the raw material pump;
oil at an oil outlet of the low-pressure separator enters a fractionation system, and the fractionation system comprises a light component removal tower and a normal hexane removal tower; the oil outlet of the low-pressure separator is connected with the feed inlet of the light component removal tower, and the top of the light component removal tower is connected with a petroleum ether I outlet device through a pipeline; a side line extraction port of the light component removal tower is connected with a feed inlet of the n-hexane removal tower, and a bottom oil outlet of the light component removal tower is connected with a petroleum ether III outlet device through a pipeline; the top of the normal hexane removal tower is connected with an isohexane outlet device through a pipeline, and the bottom of the normal hexane removal tower is connected with a normal hexane outlet device through a pipeline;
the light component removing tower is a clapboard tower, and the normal hexane removing tower is a plate tower.
Preferably, a vertical clapboard is arranged in the light component removing tower, the clapboard divides the light component removing tower into a main tower area and an auxiliary tower area, the auxiliary tower area is provided with a lateral line, and the lateral line is connected with the main tower area.
Preferably, in the device for producing the normal hexane and the isohexane, the raw materials are directly heated to the reaction temperature by a heat exchanger and a heater without passing through a heating furnace.
Preferably, in the device for producing n-hexane and isohexane, the heat exchange medium of the heat exchanger is the raw material and the reaction product.
Preferably, the device for producing the normal hexane and the isohexane comprises a fractionation system, wherein the fractionation system comprises a light component removal tower and a normal hexane removal tower.
Preferably, the device for producing the normal hexane and the isohexane is characterized in that the light component removal tower is a clapboard tower, the normal hexane removal tower is a plate tower, and a composite hole micro valve efficient tower plate is adopted.
Due to the adoption of the technical scheme, the utility model discloses have following superiority: the raw material and the hydrogen are mixed before entering the heat exchanger, and the raw material and the reaction product exchange heat in the heat exchanger, so that the heat exchange of the heat exchanger can be improvedThe heat efficiency is improved, and the utilization rate of the device is improved; removing H from recycle hydrogen in a recycle hydrogen desulfurization reactor2S is reused to protect the catalyst and ensure the long-period operation of the catalyst; the separation system introduces the baffle tower, and the baffle tower can carry out internal energy integration with many tower systems, and single tower realizes the function of two towers, improves product separation precision, improves thermodynamic efficiency, has reduced the required energy consumption of process, adopts baffle tower technique, saves a rectifying column and auxiliary equipment, has reduced equipment investment and area. The device for producing the normal hexane and the isohexane is simple and easy to operate, low in energy consumption, good in separation effect, high in thermodynamic efficiency and capable of separating four types of products simultaneously.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: 1-raw product heat exchanger (heat exchanger); 2-a heater; 3-a hydrogenation reactor; 4-a recycle hydrogen desulfurization reactor; 5-a reaction product cooler, 6-a low-pressure separator; 7-circulating hydrogen separation tank; 8-recycle hydrogen compressor; 8.1-new hydrogen inlet pipe; 9-light component removing tower; 9.1-a separator; 10-n-hexane removal tower; 11-petroleum ether I outlet device pipeline; 12-petroleum ether iii out of the plant pipeline; 13-isohexane outlet line; 14-a normal hexane outlet device pipeline, and 15-a cooler; 16-reflux tank; 17-reflux pump.
Detailed Description
The present application is described in further detail below with reference to the accompanying drawings, but the present application is not limited to only the following embodiments.
As shown in the attached figure 1, the production device for producing normal hexane and isohexane comprises a raw material product heat exchanger 1, a heater 2, a hydrogenation reactor 3, a recycle hydrogen desulfurization reactor 4, a reaction product cooler 5, a low-pressure separator 6, a recycle hydrogen separating tank 7, a recycle hydrogen compressor 8, a light component removal tower 9 and a normal hexane removal tower 10.
A raw material inlet of the raw material product heat exchanger 1 is connected with an outlet of a raw material pump (the raw material pump is arranged on a conveying pipeline of a medium raw material and used for providing power for raw material operation, is a more conventional arrangement in the industry and is not shown in the figure for prevention), and a raw material outlet of the raw material product heat exchanger 1 is connected with a feed inlet of the heater 2 through a pipeline; the discharge hole of the heater 2 is connected with the feed inlet of the hydrogenation reactor 3 through a pipeline, the discharge hole of the hydrogenation reactor 3 is connected with the product feed inlet of the raw material product heat exchanger 1 through a pipeline, the product discharge hole of the raw material product heat exchanger 1 is connected with the feed inlet of the reaction product cooler 5 through a pipeline, and the discharge hole of the reaction product cooler 5 is connected with the feed inlet of the low-pressure separator 6 through a pipeline;
the gas outlet of the low-pressure separator 6 is connected with the gas inlet of a circulating hydrogen separating tank 7, the gas outlet of the circulating hydrogen separating tank 7 is connected with the gas inlet of a circulating hydrogen compressor 8, a fresh hydrogen inlet is connected with the gas outlet pipeline of the circulating hydrogen compressor 8, the gas outlet of the circulating hydrogen compressor 8 is connected with the inlet of a circulating hydrogen desulfurization reactor 4, and the outlet of the circulating hydrogen desulfurization reactor 4 is connected with the outlet pipeline of a raw material pump;
an oil outlet of the low-pressure separator 6 is connected with a feed inlet of a light component removal tower 9, and the top of the light component removal tower 9 is connected with a petroleum ether I outlet device pipeline 11; the side line extraction port of the light component removal tower 9 is connected with the feed inlet of the n-hexane removal tower 10, the bottom oil outlet of the light component removal tower 9 is connected with a petroleum ether III outlet device pipeline 12, the top of the n-hexane removal tower 10 is connected with an isohexane outlet device pipeline 13, and the bottom of the n-hexane removal tower 10 is connected with an n-hexane outlet device pipeline 14. In addition, as shown in the attached figure 1, the top of the light component removal tower 9 and the top of the normal hexane removal tower 10 are respectively connected with a cooler 15 and a reflux tank 16 through pipelines, the cooler is connected with the reflux tank 16 through a pipeline, the reflux tank 16 is connected with a reflux pump 17 through a pipeline, and the outlet of the reflux pump 17 is connected with two pipelines: one pipeline is connected with the tower top return line, and the other pipeline is connected with the product outlet device through a pipeline.
The light component removing tower is a clapboard tower, and the normal hexane removing tower is a plate tower; and a vertical clapboard 9.1 is arranged in the light component removal tower as the clapboard tower, and divides the light component removal tower into a main tower area and an auxiliary tower area, wherein a lateral line extraction port is led out from the auxiliary tower area and is connected with the main tower area (equivalently, one tower is used as two towers, thereby realizing the repeated separation of raw materials and improving the separation efficiency).
The specific process for producing normal hexane and isohexane by adopting the device comprises the following steps: the raw material and hydrogen are mixed and then heated to the reaction temperature through a raw material product heat exchanger 1 and a heater 2, then the mixture enters a hydrogenation reactor 3 to carry out hydrofining reaction with a catalyst, and the product after the reaction is cooled through the heat exchanger 1 and a cooler 5 and then enters a low-pressure separator 6 to carry out simple gas-liquid separation. The obtained low-fraction oil enters a light component removal tower 9 for fractionation, gas-phase components at the top of the tower enter a reflux tank 16 after being cooled by a cooler 15 (composed of a water cooler and an air cooler), a part of the gas-phase components enters the tower again as top reflux by a reflux pump 17 to provide conveying force, a part of the gas-phase components is taken as a petroleum ether I product outlet device, a side line extraction port is connected with a feed port of a n-hexane removal tower 10, and an oil outlet at the bottom of the tower is connected with a petroleum ether III outlet device pipeline 12. The gas-phase components at the top of the normal hexane removal tower 10 enter a reflux tank 16 after being cooled by a cooler 15 (composed of a water cooler and an air cooler), a part of the gas-phase components enters the tower again as top reflux by a reflux pump 17 to provide conveying force, a part of the gas-phase components is taken as isohexane to be discharged from a device, and oil at the bottom of the tower is taken as normal hexane to be discharged from the device. The side draw-off port of the subsidiary column of the light ends removal column 9 is connected to the reflux line of the main column.
The recycle hydrogen is discharged from the top of the low-pressure separator 6, enters a recycle hydrogen compressor 8 through a recycle hydrogen separating tank 7 to be pressurized, and is mixed with new hydrogen 8.1 to enter a recycle hydrogen desulfurization reactor 4 to remove H2And S, mixing hydrogen with the raw materials, and feeding the mixture into a reaction system.
The feeding pipeline or the discharging pipeline of the connecting pipeline on each equipment part can be multiple, the number of the other parts to be connected is determined according to specific needs, and the number of the other parts to be connected is not limited to one; in addition, in order to provide power for the fluidity of the medium in the pipeline, a power pump can be arranged on the pipeline, and all the power pumps are the modifications in the technical scheme.
Claims (5)
1. The utility model provides a device of production n-hexane, isohexane which characterized in that: the device comprises a raw material product heat exchanger, a heater, a hydrogenation reactor, a recycle hydrogen desulfurization reactor, a reaction product cooler, a low-pressure separator, a recycle hydrogen separation tank, a recycle hydrogen compressor, a light component removal tower and a normal hexane removal tower;
a raw material inlet of the raw material product heat exchanger is connected with a raw material pump outlet through a pipeline, and a raw material outlet of the raw material product heat exchanger is connected with a feed inlet of the heater through a pipeline; the discharge hole of the heater is connected with the feed inlet of the hydrogenation reactor through a pipeline, the discharge hole of the hydrogenation reactor is connected with the product feed inlet of the raw material product heat exchanger through a pipeline, the product discharge hole of the raw material product heat exchanger is connected with the feed inlet of the reaction product cooler through a pipeline, and the discharge hole of the reaction product cooler is connected with the feed inlet of the low-pressure separator through a pipeline;
the gas outlet of the low-pressure separator is connected with the gas inlet of the circulating hydrogen separation tank, the gas outlet of the circulating hydrogen separation tank is connected with the gas inlet of the circulating hydrogen compressor, the fresh hydrogen inlet is connected with the gas outlet pipeline of the circulating hydrogen compressor, the gas outlet of the circulating hydrogen compressor is connected with the inlet of the circulating hydrogen desulfurization reactor, and the outlet of the circulating hydrogen desulfurization reactor is connected with the outlet pipeline of the raw material pump;
oil at an oil outlet of the low-pressure separator enters a fractionation system, and the fractionation system comprises a light component removal tower and a normal hexane removal tower; the oil outlet of the low-pressure separator is connected with the feed inlet of the light component removal tower, and the top of the light component removal tower is connected with a petroleum ether I outlet device through a pipeline; a side line extraction port of the light component removal tower is connected with a feed inlet of the n-hexane removal tower, and a bottom oil outlet of the light component removal tower is connected with a petroleum ether III outlet device through a pipeline; the top of the normal hexane removal tower is connected with an isohexane outlet device through a pipeline, and the bottom of the normal hexane removal tower is connected with a normal hexane outlet device through a pipeline;
the dehydrogenation component tower is a clapboard tower, and the dehexanizer tower is a plate tower.
2. The apparatus for producing n-hexane and isohexane according to claim 1, wherein: the light component removing tower is divided into a main tower area and an auxiliary tower area by a partition plate, and the side line of the auxiliary tower of the light component removing tower is extracted and connected with the main tower.
3. The apparatus for producing n-hexane and isohexane according to claim 1, wherein: the raw materials are directly heated to the reaction temperature by a heat exchanger and a heater.
4. The apparatus for producing n-hexane and isohexane according to claim 1, wherein: the heat exchange medium of the heat exchanger is raw material and reaction product.
5. The apparatus for producing n-hexane and isohexane according to claim 1, wherein: the baffle in the plate tower adopts a composite hole micro valve high-efficiency tower plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022459941.5U CN213623926U (en) | 2020-10-29 | 2020-10-29 | Device for producing normal hexane and isohexane |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022459941.5U CN213623926U (en) | 2020-10-29 | 2020-10-29 | Device for producing normal hexane and isohexane |
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| CN213623926U true CN213623926U (en) | 2021-07-06 |
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| CN202022459941.5U Active CN213623926U (en) | 2020-10-29 | 2020-10-29 | Device for producing normal hexane and isohexane |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114540080A (en) * | 2022-03-17 | 2022-05-27 | 中国石油化工股份有限公司 | Multi-raw-material n-hexane production device and n-hexane product processing method |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114540080A (en) * | 2022-03-17 | 2022-05-27 | 中国石油化工股份有限公司 | Multi-raw-material n-hexane production device and n-hexane product processing method |
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