CN103113179A - Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene - Google Patents
Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene Download PDFInfo
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- CN103113179A CN103113179A CN2013100506131A CN201310050613A CN103113179A CN 103113179 A CN103113179 A CN 103113179A CN 2013100506131 A CN2013100506131 A CN 2013100506131A CN 201310050613 A CN201310050613 A CN 201310050613A CN 103113179 A CN103113179 A CN 103113179A
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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 invention relates to a thermal coupling method for extractive distillation of normal hexane, isohexane and benzene. A rectifying tower consists of a dehydrating tower, an isohexane tower, a normal hexane extractive distillation tower, a first solvent recovery tower, a benzene extractive distillation tower and a second solvent recovery tower. Residue of the second solvent recovery tower respectively exchange heat with fed materials of the dehydrating tower and the benzene extractive distillation tower. Residue of the first solvent recovery tower is a heating medium of a reboiler of the isohexane tower, and products at the tops of the normal hexane extractive distillation tower and the benzene extractive distillation tower enter an argil adsorbent bed via two plate heat exchangers which are of all-welded type, so that all counter-current operation is realized. One of the plate heat exchanger uses the material discharged from the argil adsorbent bed as a heating medium, and all stream heats are adequately utilized. According to the invention, the power energy of the rectifying unit is greatly reduced, the production cost of the normal hexane is lowered, and the market competitiveness is improved.
Description
Technical field
The present invention relates to a kind of thermal coupling method that can reduce normal hexane, isohexane and benzene tripping device energy consumption, relate to especially and can reduce normal hexane, isohexane and benzene extracting rectifying thermal coupling system and method.
Background technology
Normal hexane is a kind of colourless transparent liquid, is one of varsol of widespread use, is the most representative non-polar solvent.The industrial hexane solvent oil can be used in the industries such as medicine, chemical industry, macromolecular material, rubber industry and food.The huge market demand of normal hexane product.
The main method of industrial production normal hexane is: at first obtain thick normal hexane from straight run or raffinating oil with the method for rectifying or the method for platformate raffinate hydrogenation, and then make highly purified normal hexane through methods such as molecular sieve adsorption, intermittent azeotropic rectifying, extracting rectifyings.The product purity that molecular sieve adsorption obtains is high, but yield is not high.The yield of azeotropic distillation is high, but the product purity that obtains is not high.The product purity of extraction fractional distillation is higher, can reach more than 99%, has simultaneously higher yield, yet existing extraction rectification technique needs a large amount of steam to be used for heating, needs simultaneously a large amount of water coolants to be used for cooling material, and energy consumption is high.Therefore developing new technique, effectively reduce rectifying workshop section energy consumption, is the key that reduces normal hexane, isohexane and benzene tripping device production cost.
Summary of the invention
The object of the present invention is to provide a kind of thermal coupling method that can reduce normal hexane, isohexane and benzene tripping device energy consumption.This technique can reduce the consumption of steam and water coolant in production process, the energy consumption of decrease rectification cell.
According to the present invention, the technique that normal hexane, isohexane and benzene separate is as follows: from the total hydrocarbon feed outside the battery limit (BL) after the feed preheater preheating, from lightness-removing column top charging, overhead vapours is after condenser condenses, lime set enters a return tank part and refluxes, another part as the light constituent product from the return tank extraction; Remove than 2-methylpentane after low-boiling impurity composition through lightness-removing column, send into the isohexane tower and remove the low-boiling cut of isohexane geometric ratio normal hexane, overhead extraction stream thigh is sent into basin as the isohexane product; Isohexane tower reactor extraction material is sent into the n-hexane extraction rectifying tower and is separated, and extraction agent adds by above feed plate, obtains normal hexane product after the normal hexane stream stock-traders' know-how bleaching earth adsorption bed of overhead extraction is processed and sends into basin; The tower reactor extraction; Mixture is sent into the first solvent recovery tower and is separated, and tower reactor is recycled solvent, most of return to normal hexane get the rectifying tower Reusability after cooling, and it is assorted that small part is sent the solvent reclamation unit to take off to reset; Tower top obtains the mixture of benzene and non-aromatics impurity; The first solvent recuperation tower top stream thigh is sent into the benzene extractive distillation column and is separated, and extraction agent adds by above feed plate, from removed overhead non-aromatics impurity, and sends into basin as the solvent oil product; Tower reactor is the mixed flow thigh of benzene and extraction agent, send the second solvent recovery tower to separate; The second solvent recuperation tower reactor is recycled solvent, most of returns to benzene extractive distillation column Reusability after cooling, and it is assorted that small part is sent the solvent reclamation unit to take off to reset; After the benzene stream stock-traders' know-how bleaching earth adsorption bed of overhead extraction is processed, obtain benzaldehyde product.
Technical scheme of the present invention is as follows:
A kind of normal hexane, isohexane and the hot coupling of benzene abstraction distillation system system get rectifying tower 108, the first solvent recovery tower 113, benzene extractive distillation column 116 and the second solvent recovery tower 118 by lightness-removing column 101, isohexane purification tower 105, normal hexane and form; Each tower bottom is provided with reboiler; It is characterized in that being provided with before lightness-removing column 101 feed preheater 103, the second solvent recovery tower 118 tower reactors, the feed preheater 103 of lightness-removing column, feed preheater 104 is connected successively with benzene extractive distillation column 116; The tower reactor of isohexane purification tower 105 is provided with the reboiler 107 of tower reactor, the isohexane purification tower of reboiler 107, the first solvent recovery towers 113 of isohexane purification tower, solvent cooler 115 and normal hexane that normal hexane is got rectifying tower are got rectifying tower 108 and be connected successively; The tower top, feed preheater 104 and the benzene extractive distillation column 116 that are provided with charging plate-type heat exchanger 104, the first solvent recovery towers 113 before benzene extractive distillation column 116 are connected successively; Normal hexane is got rectifying tower 108, normal hexane the first plate-type heat exchanger 109, normal hexane the second plate-type heat exchanger 110 and is connected successively with normal hexane bleaching earth adsorption bed 111, and normal hexane bleaching earth adsorption bed 111 is connected with normal hexane the first plate-type heat exchanger 109 and forms the loop; The second solvent recovery tower 118, crude benzol the first plate-type heat exchanger 119, crude benzol the second plate-type heat exchanger 120 are connected successively with crude benzol bleaching earth adsorption bed 121, and crude benzol bleaching earth adsorption bed 121 is connected with crude benzol the first plate-type heat exchanger 119 and forms the loop.
isohexane of the present invention, normal hexane and benzene abstraction distillation system thermal coupling method, raw material enters the tube side of the feed preheater 103 of lightness-removing column, the still liquid of the second solvent recovery tower 118 tower reactors enters the shell side of the feed preheater 103 of lightness-removing column, through heat exchange, raw material enters lightness-removing column 101, still liquid continues to enter the charging plate-type heat exchanger 104 of benzene extractive distillation column, overhead gas to the first solvent recovery tower 113 heats, after heat exchange, the still liquid stream thigh of the second solvent recovery tower 118 tower reactors and the overhead gas stream thigh of the first solvent recovery tower 113 all enter benzene extractive distillation column 116, isohexane purification tower 105 has two reboilers, adopt shell and tube heat exchanger, wherein, the still liquid of isohexane purification tower 105 is back to isohexane tower 105 through the shell side of isohexane tower reboiler 107, the still liquid of the first solvent recovery tower 113 enters the tube side of isohexane tower reboiler 107, still liquid to isohexane purification tower 105 heats, and the solvent cooler 115 that heat exchange is got rectifying tower by normal hexane enters to normal hexane and gets rectifying tower 108, the overhead product of n-hexane extraction rectifying tower 108 enters normal hexane bleaching earth adsorption bed after two plate-type heat exchangers, the overhead product of n-hexane extraction rectifying tower 108 is first heated by the discharging of normal hexane bleaching earth adsorption bed, then is heated by thermal oil, enters normal hexane bleaching earth adsorption bed after twice heat exchange, the overhead product of the second solvent recovery tower 118 enters crude benzol bleaching earth adsorption bed after two plate-type heat exchangers, the overhead product of the second solvent recovery tower 118 is first heated by the discharging of crude benzol bleaching earth adsorption bed, heated by thermal oil again, enter crude benzol bleaching earth adsorption bed after twice heat exchange.
Described plate-type heat exchanger adopts full-welding plate-type heat exchanger.
In the present invention, the still liquid of the second solvent recovery tower carries out heat exchange with the charging of lightness-removing column and benzene extractive distillation column respectively, the still liquid of the first solvent recovery tower is the heating medium of isohexane tower reboiler, the overhead product of n-hexane extraction rectifying tower and benzene extractive distillation column enters the bleaching earth adsorption bed after two plate-type heat exchangers, plate-type heat exchanger adopts full-welding plate-type heat exchanger, can realize full counter-current operation, one of them plate-type heat exchanger adopts the discharging of bleaching earth adsorption bed as heating medium, takes full advantage of each stream strand heat.Carry out heat exchange between different material stream, heat of each stream in this process strand is taken full advantage of, reduced the consumption of steam and water coolant in isohexane, normal hexane and benzene extracting rectifying process, reduced the normal hexane production cost, improved the market competitiveness.
Description of drawings
Fig. 1: isohexane, normal hexane and benzene abstraction distillation system thermal coupling method flow schematic diagram.
Embodiment
Below in conjunction with accompanying drawing, several connections of the present invention are described in further detail.
A kind of normal hexane, isohexane and the hot coupling of benzene abstraction distillation system system get rectifying tower 108, the first solvent recovery tower 113, benzene extractive distillation column 116 and the second solvent recovery tower 118 by lightness-removing column 101, isohexane purification tower 105, normal hexane and form; Each tower bottom is provided with reboiler; It is characterized in that being provided with before lightness-removing column 101 feed preheater 103, the second solvent recovery tower 118 tower reactors, the feed preheater 103 of lightness-removing column, feed preheater 104 is connected successively with benzene extractive distillation column 116; The tower reactor of isohexane purification tower 105 is provided with the reboiler 107 of tower reactor, the isohexane purification tower of reboiler 107, the first solvent recovery towers 113 of isohexane purification tower, solvent cooler 115 and normal hexane that normal hexane is got rectifying tower are got rectifying tower 108 and be connected successively; The tower top, feed preheater 104 and the benzene extractive distillation column 116 that are provided with charging plate-type heat exchanger 104, the first solvent recovery towers 113 before benzene extractive distillation column 116 are connected successively; Normal hexane is got rectifying tower 108, normal hexane the first plate-type heat exchanger 109, normal hexane the second plate-type heat exchanger 110 and is connected successively with normal hexane bleaching earth adsorption bed 111, and normal hexane bleaching earth adsorption bed 111 is connected with normal hexane the first plate-type heat exchanger 109 and forms the loop; The second solvent recovery tower 118, crude benzol the first plate-type heat exchanger 119, crude benzol the second plate-type heat exchanger 120 are connected successively with crude benzol bleaching earth adsorption bed 121, and crude benzol bleaching earth adsorption bed 121 is connected with crude benzol the first plate-type heat exchanger 119 and forms the loop.
Raw material enters lightness-removing column 101 through feed preheater 103, and the heating medium of feed preheater 103 is the still liquid of the second solvent recovery tower 120.The still liquid of the second solvent recovery tower 118 enters benzene extractive distillation column 116 after the feed preheater 103 of lightness-removing column 101 feed preheater 104 carries out thermal coupling again, and the charging of benzene extractive distillation column 116 is heated.
Isohexane tower 105 adopts the mode of two reboiler heating.Wherein the heating medium of reboiler 106 is live steam, and the heating medium of reboiler 107 is the still liquid of the first solvent recovery tower 113.The still liquid of the first solvent recovery tower 113 enters n-hexane extraction rectifying tower 108, the first solvent recovery tower 113 still liquid after water cooler 107 and water cooler 115 water cooler 107 is same equipment with isohexane tower reboiler 107.The heat-eliminating medium of water cooler 115 is recirculated water.
The overhead product of n-hexane extraction rectifying tower 108 enters normal hexane bleaching earth adsorption bed 111 after normal hexane the first preheater 109 and normal hexane the second preheater 110 heating.The hot-fluid thigh of normal hexane the first preheater 109 is originated and is the discharging of normal hexane bleaching earth adsorption bed 111, and the hot-fluid thigh of normal hexane the second preheater 110 is originated and is thermal oil.Normal hexane the first preheater 109 and normal hexane the second preheater 110 are full-welding plate-type heat exchanger, can realize full counter-current operation, fully reclaim heat.
The overhead product of the second solvent recovery tower 118 enters crude benzol bleaching earth adsorption bed 121 after crude benzol the first preheater 119 and crude benzol the second preheater 120 heating.The hot-fluid thigh of crude benzol the first preheater 119 is originated and is the discharging of crude benzol bleaching earth adsorption bed 121, and the hot-fluid thigh of crude benzol the second preheater 120 is originated and is thermal oil.Crude benzol the first preheater 119 and crude benzol the second preheater 120 are full-welding plate-type heat exchanger, can realize full counter-current operation, fully reclaim heat.
Claims (3)
1. a normal hexane, isohexane and the hot coupling of benzene abstraction distillation system system, get rectifying tower (108), the first solvent recovery tower (113), benzene extractive distillation column (116) and the second solvent recovery tower (118) by lightness-removing column (101), isohexane purification tower (105), normal hexane and form; Each tower bottom is provided with reboiler; It is characterized in that the front feed preheater (103) that is provided with of lightness-removing column (101), being connected successively of the feed preheater (103) of the second solvent recovery tower (118) tower reactor, lightness-removing column, feed preheater (104) and benzene extractive distillation column (116); The tower reactor of isohexane purification tower (105) is provided with the reboiler (107) of isohexane purification tower, and the solvent cooler (115) that the reboiler (107) of the tower reactor of the first solvent recovery tower (113), isohexane purification tower, normal hexane are got rectifying tower is got rectifying tower (108) with normal hexane and is connected successively; The front charging plate-type heat exchanger (104) that is provided with of benzene extractive distillation column (116), the tower top of the first solvent recovery tower (113), feed preheater (104) and benzene extractive distillation column (116) are connected successively; Normal hexane is got rectifying tower (108), normal hexane the first plate-type heat exchanger (109), normal hexane the second plate-type heat exchanger (110) and normal hexane bleaching earth adsorption bed (111) and is connected successively, and normal hexane bleaching earth adsorption bed (111) is connected with normal hexane the first plate-type heat exchanger (109) and forms the loop; The second solvent recovery tower (118), crude benzol the first plate-type heat exchanger (119), crude benzol the second plate-type heat exchanger (120) and crude benzol bleaching earth adsorption bed (121) are connected successively, and crude benzol bleaching earth adsorption bed (121) is connected with crude benzol the first plate-type heat exchanger (119) and forms the loop.
2. isohexane as claimed in claim 1, normal hexane and benzene abstraction distillation system thermal coupling method, it is characterized in that raw material enters the tube side of the feed preheater of lightness-removing column (103), the still liquid of the second solvent recovery tower (118) tower reactor enters the shell side of the feed preheater (103) of lightness-removing column, through heat exchange, raw material enters lightness-removing column (101), still liquid continues to enter the charging plate-type heat exchanger (104) of benzene extractive distillation column, overhead gas to the first solvent recovery tower (113) heats, after heat exchange, the still liquid stream thigh of the second solvent recovery tower (118) tower reactor and the overhead gas stream thigh of the first solvent recovery tower (113) all enter benzene extractive distillation column (116), isohexane purification tower (105) has two reboilers, adopt shell and tube heat exchanger, wherein, the still liquid of isohexane purification tower (105) is back to isohexane tower (105) through the shell side of isohexane tower reboiler (107), the still liquid of the first solvent recovery tower (113) enters the tube side of isohexane tower reboiler (107), still liquid to isohexane purification tower (105) heats, and the solvent cooler (115) that heat exchange is got rectifying tower by normal hexane enters to normal hexane and gets rectifying tower (108), the overhead product of n-hexane extraction rectifying tower (108) enters normal hexane bleaching earth adsorption bed after two plate-type heat exchangers, the overhead product of n-hexane extraction rectifying tower (108) is first heated by the discharging of normal hexane bleaching earth adsorption bed, then is heated by thermal oil, enters normal hexane bleaching earth adsorption bed after twice heat exchange, the overhead product of the second solvent recovery tower (118) enters crude benzol bleaching earth adsorption bed after two plate-type heat exchangers, the overhead product of the second solvent recovery tower (118) is first heated by the discharging of crude benzol bleaching earth adsorption bed, heated by thermal oil again, enter crude benzol bleaching earth adsorption bed after twice heat exchange.
3. isohexane as claimed in claim 2, normal hexane and benzene abstraction distillation system thermal coupling method, is characterized in that plate-type heat exchanger adopts full-welding plate-type heat exchanger.
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| CN201310050613.1A CN103113179B (en) | 2013-02-07 | 2013-02-07 | Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene |
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| CN201310050613.1A CN103113179B (en) | 2013-02-07 | 2013-02-07 | Thermal coupling system and method for extractive distillation of normal hexane, isohexane and benzene |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242120A (en) * | 2013-04-27 | 2013-08-14 | 天津大学 | Circulating device and refining method of extractant in normal hexane, isohexane and benzene separation process |
| CN107189854A (en) * | 2017-05-28 | 2017-09-22 | 天津大学 | Vapor recompression and the integrated microalgae grease extracting system of heat exchange |
| CN117883810A (en) * | 2024-03-14 | 2024-04-16 | 潍坊三昌化工科技有限公司 | Mixed pentane precise separation device |
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| CN101734998A (en) * | 2009-12-22 | 2010-06-16 | 南京师范大学 | Method for extracting trimethylbenzene fraction in hydrocracking C9 by combined solvent extraction rectification method |
| CN102351627A (en) * | 2011-09-07 | 2012-02-15 | 洛阳金达石化有限责任公司 | Process method for extracting normal hexane and isohexane from crude hexane |
| CN102675029A (en) * | 2012-02-25 | 2012-09-19 | 中国石油大学(华东) | Method for separating methylcyclohexane and toluene through differential pressure thermal coupling extractive rectification |
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| CN101234947A (en) * | 2008-02-15 | 2008-08-06 | 南京大学 | Method for removing micro-benzene in solvent oil or hexane refining process |
| CN101734998A (en) * | 2009-12-22 | 2010-06-16 | 南京师范大学 | Method for extracting trimethylbenzene fraction in hydrocracking C9 by combined solvent extraction rectification method |
| CN102351627A (en) * | 2011-09-07 | 2012-02-15 | 洛阳金达石化有限责任公司 | Process method for extracting normal hexane and isohexane from crude hexane |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103242120A (en) * | 2013-04-27 | 2013-08-14 | 天津大学 | Circulating device and refining method of extractant in normal hexane, isohexane and benzene separation process |
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| CN107189854A (en) * | 2017-05-28 | 2017-09-22 | 天津大学 | Vapor recompression and the integrated microalgae grease extracting system of heat exchange |
| CN107189854B (en) * | 2017-05-28 | 2023-10-31 | 天津大学 | Microalgae grease extraction system integrating vapor recompression and heat exchange |
| CN117883810A (en) * | 2024-03-14 | 2024-04-16 | 潍坊三昌化工科技有限公司 | Mixed pentane precise separation device |
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