CN101602641B - Double-effect rectification method and system thereof for finely separating hybrid pentane isomer - Google Patents
Double-effect rectification method and system thereof for finely separating hybrid pentane isomer Download PDFInfo
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- CN101602641B CN101602641B CN 200910069668 CN200910069668A CN101602641B CN 101602641 B CN101602641 B CN 101602641B CN 200910069668 CN200910069668 CN 200910069668 CN 200910069668 A CN200910069668 A CN 200910069668A CN 101602641 B CN101602641 B CN 101602641B
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- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical class CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 title claims abstract description 108
- 238000000034 method Methods 0.000 title claims abstract description 31
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims abstract description 145
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims abstract description 72
- RGSFGYAAUTVSQA-UHFFFAOYSA-N Cyclopentane Chemical compound C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 claims abstract description 44
- 238000010992 reflux Methods 0.000 claims abstract description 22
- 239000002994 raw material Substances 0.000 claims abstract description 17
- 239000000203 mixture Substances 0.000 claims abstract description 9
- 239000002918 waste heat Substances 0.000 claims abstract description 7
- 125000004817 pentamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 claims description 32
- 241000282326 Felis catus Species 0.000 claims description 21
- 238000000926 separation method Methods 0.000 claims description 19
- HNRMPXKDFBEGFZ-UHFFFAOYSA-N 2,2-dimethylbutane Chemical compound CCC(C)(C)C HNRMPXKDFBEGFZ-UHFFFAOYSA-N 0.000 claims description 18
- 238000004821 distillation Methods 0.000 claims description 11
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims description 6
- 239000012530 fluid Substances 0.000 claims description 6
- 238000009834 vaporization Methods 0.000 claims description 6
- 230000008016 vaporization Effects 0.000 claims description 6
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 5
- 238000009833 condensation Methods 0.000 abstract description 3
- 230000005494 condensation Effects 0.000 abstract description 3
- 238000006356 dehydrogenation reaction Methods 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 abstract 3
- 238000010009 beating Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 20
- 230000008569 process Effects 0.000 description 17
- 238000000605 extraction Methods 0.000 description 12
- 239000000463 material Substances 0.000 description 8
- 238000011084 recovery Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000004088 foaming agent Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229920001684 low density polyethylene Polymers 0.000 description 1
- 239000004702 low-density polyethylene Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
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Abstract
The invention discloses a double-effect rectification method for finely separating hybrid pentane isomer, which comprises the following steps: introducing a crude pentane raw material into a condensation preheater, a dehydrogenation tower of which the top is connected with a condenser and a reflux tank and the bottom is connected with a reboiler, an isopentane tower, an n-pentane tower, an azeotrope tower and a cyclopentane tower in turn to be rectified and separated, feeding total vapor at the tower top of the isopentane tower into the n-pentane tower and the reboiler as heat sources thereof, condensing the vapor into a two-phase mixture of vapor and liquid after heat exchange, then feeding the mixture to the azeotrope tower and the reboiler to exchange heat, re-preheating the crude pentane raw material by the waste heat after heat exchange, and finally beating the liquid to the isopentane tower as reflux liquid by a reflux pump of the isopentane tower. The method has the advantages of high product purity and low energy consumption and water consumption; and the product can be flexibly controlled according to the requirement.
Description
Technical field
The present invention relates to a kind of Chemicals purification technique field, particularly the double-effect rectification energy-saving and water-saving system and the technology of pentane isomer fine separation.
Background technology
Pentane is a kind of very important Chemicals; Can be used as the whipping agent of eps (EPS), expandability Vilaterm (EPE) and year solvent of line low density polyethylene catalyst; In addition; Can also be used for industries such as pottery as pentane fuel, from consumption structure, it is the consumption maximum in the whipping agent field.The main production raw material of pentane is light naphthar, the hydrocarbon mixture behind the reformation hydrogenation of tops, the hydrogenation unit of oil field light hydrocarbon, crude oil upgrading device, the C of refinery's gas separation unit
5And the C of ethylene unit cracking by-product
5Cut.At present, supply exceed demand on the whole for domestic pentane, but high-quality product is seriously under-supply, has very big market has openings.Rectifying is very important chemical engineering unit operation during pentane is produced; Be directly connected to the problems such as quality, environment protection, energy consumption and production cost of product; So advanced rectification process is to promote the important technical links that pentane production further develops, and more and more causes people's attention.
The existing pentane isomer tripping device of China as shown in Figure 1 all is the four tower continuous rectification flow processs that adopt single-action, and crude pentane is connected with lightness-removing column 1, its top that condensing surface 7-1 and return tank 6-1, bottom be connected with reboiler 8-1 through condensate preheater 5, its top successively and is connected with iso-pentane tower 2, its top that condensing surface 7-2 and return tank 6-2, bottom be connected with reboiler 8-2 and is connected with Skellysolve A tower 3, its top that condensing surface 7-3 and return tank 6-3, bottom be connected with reboiler 8-3 and is connected with pentamethylene tower 4 that condensing surface 7-4 and return tank 6-4, bottom be connected with reboiler 8-4 and carries out rectifying separation and handle.Described lightness-removing column 1 top extraction light constituent (being rich in C-4-fraction), qualified tower bottom distillate get into iso-pentane tower 2 middle parts.Described iso-pentane cat head extraction iso-pentane product takes out the cut that is rich in Skellysolve A and pentamethylene and sends into described Skellysolve A tower 3 at the bottom of the tower.Described Skellysolve A tower 3 top of tower extraction Skellysolve As; The cut that is rich in pentamethylene that take out the bottom is sent into described pentamethylene tower 4; Described pentamethylene column overhead extraction pentamethylene, component impurity in taking out at the bottom of the tower is though this process method has advantages such as flow process is simple, easy to operate, stable; But energy expenditure is big, and quality product is not high.
Summary of the invention
The objective of the invention is to overcome the deficiency of prior art, provide a kind of product purity height, energy consumption, water to consume the double-effect distillation method and the system thereof of low, that product can be controlled as requested flexibly a kind of hybrid pentane isomer fine separation.
The double-effect distillation method of a kind of hybrid pentane isomer fine separation of the present invention, it may further comprise the steps:
The raw material crude pentane carries out rectifying separation through condensate preheater, lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, pentamethylene tower successively to be handled; The top of each tower all is connected with condensing surface and return tank, bottom all are connected with reboiler in described lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, the pentamethylene tower; Whole steam of the cat head of wherein said iso-pentane tower are sent into Skellysolve A tower reboiler as its thermal source; Be condensed into gas-fluid two-phase mixture after the heat exchange; It is sent into the azeotrope column reboiler carry out heat exchange, the waste heat after the heat exchange is the described raw material crude pentane of preheating again, is returned as iso-pentane tower phegma by iso-pentane tower reflux pump at last; The cat head working pressure of described iso-pentane tower is 630kPa-650kPa; The overhead vapours temperature is 95 ℃-100 ℃, is 95 ℃-100 ℃ through temperature behind the Skellysolve A tower reboiler, is 55 ℃-86 ℃ through temperature behind the reboiler of azeotrope column; Through temperature behind the condensate preheater is 50 ℃-80 ℃, and the temperature of the raw material after preheating is 45 ℃-75 ℃; The theoretical stage of described azeotrope column is 70-80; Working pressure 160kPa-180kPa, reflux ratio is 90-100,63 ℃-66 ℃ of tower top temperatures; And the mass ratio that its cat head neohexane and hexanaphthene take out is 1: 2.21～1: 2.23, and the vaporization rate of described Skellysolve A tower bottom reboiler is 0.25.
The system of the double-effect rectification of a kind of hybrid pentane isomer fine separation of the present invention; It comprises condensate preheater, lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, the pentamethylene tower that discharge port and opening for feed link to each other through pipeline successively; The top of each tower all is connected with condensing surface and return tank, bottom all are connected with reboiler in described lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, the pentamethylene tower; Link to each other through the feeding mouth of first outlet line at the bottom of the tower of described Skellysolve A tower with described azeotrope column middle part; The discharge port of described azeotrope column bottom links to each other with the feeding mouth at the middle part of described pentamethylene tower through second outlet line, and the cat head of described iso-pentane tower passes through reboiler, the condensate preheater of reboiler, the azeotrope column of the 3rd outlet line and Skellysolve A tower, the overhead condenser of iso-pentane tower links to each other successively.
The present invention has following advantage:
With the cryogenic condensation heat of iso-pentane column overhead successively as the thermal source of Skellysolve A tower reboiler, azeotrope column reboiler and feed preheater, thereby form " double-effect rectification ", the step of realizing energy reclaims and utilizes; Between Skellysolve A knockout tower and pentamethylene knockout tower, increase azeotrope column and improve the cyclopentane product quality.Find through analyzing; Usually contain impurity such as neohexane in the crude pentane raw material, its boiling point and pentamethylene are very approaching, use single tower to be difficult for realizing fine separation; It is the principal element that influences the cyclopentane product quality; So this technology increases azeotrope column,, therefore can it be extracted out from the azeotrope column cat head through calculating the neohexane of discovery more than 94% in the enrichment of azeotrope column cat head; Thereby make qualified tower bottom distillate get into the pentamethylene tower and isolate high-quality cyclopentane product, the cut of extraction can go out system or return the raw material surge tank.
2. process of the present invention is reasonable in design; Can control product extraction form flexibly, fully reasonable use be difficult to the cryogenic condensation heat utilized in the process, make the steam consumption of whole device can fall 25%-30% than existing procedure; Cooling water consumption reduces 25%-30%; Really accomplish energy-saving and water-saving, and removed key impurity such as neohexane, further improved the cyclopentane product quality.
Description of drawings
Fig. 1 is existing pentane isomer rectification process schematic flow sheet;
Fig. 2 is the process flow diagram of the double-effect distillation method of a kind of pentane isomer fine separation of the present invention.
Embodiment
Describe the present invention below in conjunction with accompanying drawing and specific embodiment.
The double-effect distillation method of of the present invention a kind of hybrid pentane isomer fine separation as shown in Figure 2; It may further comprise the steps: the raw material crude pentane is connected with lightness-removing column 1, its top that condensing surface 7-1 and return tank 6-1, bottom be connected with reboiler 8-1 through condensate preheater 10, its top successively and is connected with iso-pentane tower 2, its top that the second condensing surface 7-2 and return tank 6-2, bottom be connected with reboiler 8-2 and is connected with Skellysolve A tower 3, its top that condensing surface 7-3 and return tank 6-3, bottom be connected with reboiler 8-3 and is connected with azeotrope column 5, its top that condensing surface 7-5 and return tank 6-5, bottom be connected with reboiler 8-5 and is connected with pentamethylene tower 4 that condensing surface 7-4 and return tank 6-4, bottom be connected with reboiler 8-4 and carries out rectifying separation and handle; Whole steam of the cat head of wherein said iso-pentane tower 2 are sent into Skellysolve A tower reboiler 8-3 as its thermal source; Be condensed into gas-fluid two-phase mixture after the heat exchange; It is sent into azeotrope column reboiler 8-5 carry out heat exchange; Waste heat after the heat exchange is the described raw material crude pentane of preheating again; Return as iso-pentane tower phegma by iso-pentane tower reflux pump at last; The cat head working pressure of described iso-pentane tower is 630kPa-650kPa; The overhead vapours temperature is 95 ℃-100 ℃, is 95 ℃-100 ℃ through temperature behind the Skellysolve A tower reboiler 8-3, is 55 ℃-86 ℃ through temperature behind the reboiler 8-5 of azeotrope column; Through temperature after condensate preheater 10 heat exchange is 50 ℃-80 ℃, and the temperature of the raw material after preheating is 45 ℃-75 ℃; The theoretical stage of described azeotrope column is 70-80; Cat head working pressure 160kPa-180kPa; Reflux ratio is 90-100; 63 ℃-66 ℃ of tower top temperatures, and the mass ratio that its cat head neohexane and hexanaphthene take out is 1: 2.21～1: 2.23, and the vaporization rate of described Skellysolve A tower bottom reboiler 8-3 is 0.25.A whole set of technology is except producing highly purified iso-pentane, Skellysolve A and cyclopentane product; Also can realize " fixing output quota by sales "; The direct production certain proportion mixes positive iso-pentane whipping agent; Just under the constant situation of whole device, through adjusting process parameter (like temperature, pressure, reflux ratio) can be directly (such as iso-pentane: Skellysolve A=7: 3 or iso-pentane: hybrid pentane whipping agent Skellysolve A=5: 5) is as production marketing from iso-pentane column overhead extraction certain proportion.Lightness-removing column in this process method, Skellysolve A tower and pentamethylene tower adopt the processing parameter control of the routine in the existing technical process to get final product.
The system of the double-effect distillation method of hybrid pentane isomer fine separation of the present invention; It comprises that condensate preheater 10, its top that discharge port and opening for feed link to each other through pipeline successively are connected with lightness-removing column 1, its top that condensing surface 7-1 and return tank 6-1, bottom be connected with reboiler 8-1 and are connected with iso-pentane tower 2, its top that condensing surface 7-2 and return tank 6-2, bottom be connected with reboiler 8-2 and are connected with Skellysolve A tower 3 that condensing surface 7-3 and return tank 6-3, bottom be connected with reboiler 8-3, are connected between described Skellysolve A tower 3, the pentamethylene tower 4 and its top is connected with the azeotrope column 5 that condensing surface 7-5 and return tank 6-5, bottom are connected with reboiler 8-5; Link to each other with the feeding mouth at described azeotrope column 5 middle parts through first outlet line at the bottom of the tower of described Skellysolve A tower 3; The discharge port of described azeotrope column 5 bottoms links to each other with the feeding mouth at the middle part of described pentamethylene tower 4 through second outlet line, and the cat head of described iso-pentane tower 2 passes through reboiler 8-3,8-5, the condensate preheater 10 of the 3rd outlet line and Skellysolve A tower and azeotrope column, the overhead condenser 7-2 of iso-pentane tower links to each other successively.
Embodiment 1
The year treatment capacity of carbon Wuyuan material is 4 * 10
4Kilogram, isopentane content 35% (wt%, as follows), Skellysolve A content 50%; Pentamethylene content 5%, iso-pentane tower extraction 99% iso-pentane product, temperature is 72 ℃ behind the raw material preheating, lightness-removing column tower top pressure 540kPa; 54 ℃ of tower top temperatures, iso-pentane column overhead pressure 650kPa, 95 ℃ of tower top temperatures, reflux ratio 11; Skellysolve A column overhead pressure 195kPa, 57 ℃ of tower top temperatures, reflux ratio 3.8, described Skellysolve A tower bottom reboiler 8-3 vaporization rate be 0.25.Azeotrope column tower top pressure 175kPa, 66 ℃ of tower top temperatures, theoretical stage are 70; Reflux ratio is 100, and the mass ratio that its cat head neohexane and hexanaphthene take out is 1: 2.23, pentamethylene column overhead pressure 185kPa; 69 ℃ of tower top temperatures, whole steam of iso-pentane cat head are sent into Skellysolve A tower reboiler as its thermal source, are condensed into gas-fluid two-phase mixture after the heat exchange; It is sent into the azeotrope column reboiler carry out heat exchange, the waste heat after the heat exchange is preheating material again, is returned as iso-pentane tower phegma by iso-pentane tower reflux pump at last; Isopentane separation tower working pressure is 630kPa, and the overhead vapours temperature is 95 ℃, is 95 ℃ through temperature behind the Skellysolve A reboiler; Through temperature behind the azeotrope column reboiler is 86 ℃, is 80 ℃ through temperature behind the condensate preheater.
Through behind the said process, main products iso-pentane purity is 99%, and the recovery is 99.5%; Skellysolve A purity is 99.3%, the recovery is 99.3%; Pentamethylene purity is 98.4%, and the recovery is 81%, and it is about 27% that whole flow process is saved steam than the single-action distillation process, circulating condensing water about 27%.
Embodiment 2
The year treatment capacity of carbon Wuyuan material is 4 * 10
4Kilogram, isopentane content 35% (wt%, as follows), Skellysolve A content 50%; Pentamethylene content 5%, 5: 5 positive iso-pentane mixed foaming agent products of iso-pentane tower extraction mass ratio, temperature is 45 ℃ behind the raw material preheating, dehydrogenation column overhead pressure 540kPa; 54 ℃ of tower top temperatures, iso-pentane column overhead pressure 650kPa, 100 ℃ of temperature, reflux ratio 1.7; Skellysolve A column overhead pressure 195kPa, 57 ℃ of tower top temperatures, reflux ratio 4.5, the vaporization rate of described Skellysolve A tower bottom reboiler is 0.25.Azeotrope column tower top pressure 180kPa, 63 ℃ of tower top temperatures, theoretical stage are 75; Reflux ratio is 95, and the mass ratio that its cat head neohexane and hexanaphthene take out is 1: 2.21, pentamethylene column overhead pressure 185kPa; 69 ℃ of tower top temperatures, whole steam of iso-pentane cat head are sent into Skellysolve A tower reboiler as its thermal source, are condensed into gas-fluid two-phase mixture after the heat exchange; It is sent into the azeotrope column reboiler carry out heat exchange, the waste heat after the heat exchange is preheating material again, is returned as iso-pentane tower phegma by iso-pentane tower reflux pump at last; Isopentane separation column overhead working pressure is 650kPa, and the overhead vapours temperature is 100 ℃, is 99.5 ℃ through temperature behind the Skellysolve A reboiler; Through temperature behind the azeotrope column reboiler is 55 ℃, is 50 ℃ through temperature behind the condensate preheater.
Through behind the said process, the positive iso-pentane mixed foaming agent of main products purity is 99%, and the iso-pentane recovery is 99.8%; The Skellysolve A product purity is 99.2%, and Skellysolve A recycled in its entirety rate is 99.9%; Pentamethylene purity is 98.4%, and the recovery is 80%, and it is about 50% that whole flow process is saved steam than the single-action distillation process of iso-pentane tower list material extraction, circulating condensing water about 50%.
Embodiment 3
The year treatment capacity of carbon Wuyuan material is 4 * 10
4Kilogram, isopentane content 35% (wt%, as follows), Skellysolve A content 50%; Pentamethylene content 5%, 3: 7 positive iso-pentane mixed foaming agent products of iso-pentane tower extraction mass ratio, temperature is 45 ℃ behind the raw material preheating, dehydrogenation column overhead pressure 540kPa; 54 ℃ of tower top temperatures, iso-pentane column overhead pressure 650kPa, 100 ℃ of temperature, reflux ratio 1.7; Skellysolve A column overhead pressure 195kPa, 57 ℃ of tower top temperatures, reflux ratio 4.5, the vaporization rate ratio of described Skellysolve A tower bottom reboiler 8-3 is 0.25.Azeotrope column tower top pressure 160kPa, 65 ℃ of tower top temperatures, theoretical stage are 80; Reflux ratio is 90, and the mass ratio that its cat head neohexane and hexanaphthene take out is 1: 2.22, pentamethylene column overhead pressure 185kPa; 69 ℃ of tower top temperatures, whole steam of iso-pentane cat head are sent into Skellysolve A tower reboiler as its thermal source, are condensed into gas-fluid two-phase mixture after the heat exchange; It is sent into the azeotrope column reboiler carry out heat exchange, the waste heat after the heat exchange is preheating material again, is returned as iso-pentane tower phegma by iso-pentane tower reflux pump at last; Isopentane separation tower working pressure is 640kPa, and the overhead vapours temperature is 98 ℃, is 97 ℃ through temperature behind the Skellysolve A reboiler; Through temperature behind the azeotrope column reboiler is 70 ℃, is 60 ℃ through temperature behind the condensate preheater.
Through behind the said process, the positive iso-pentane mixed foaming agent of main products purity is 99%, and the iso-pentane recovery is 99.8%; The Skellysolve A product purity is 99.2%, and Skellysolve A recycled in its entirety rate is 99.9%; Pentamethylene purity is 98.4%, and the recovery is 80%, and it is about 50% that whole flow process is saved steam than the single-action distillation process of iso-pentane tower list material extraction, circulating condensing water about 50%.
Claims (2)
1. the double-effect distillation method of a hybrid pentane isomer fine separation is characterized in that it may further comprise the steps:
The raw material crude pentane carries out rectifying separation through condensate preheater, lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, pentamethylene tower successively to be handled; The top of each tower all is connected with condensing surface and return tank, bottom all are connected with reboiler in described lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, the pentamethylene tower; Whole steam of the cat head of wherein said iso-pentane tower are sent into Skellysolve A tower reboiler as its thermal source; Be condensed into gas-fluid two-phase mixture after the heat exchange; It is sent into the azeotrope column reboiler carry out heat exchange, the waste heat after the heat exchange is the described raw material crude pentane of preheating again, is returned as iso-pentane tower phegma by iso-pentane tower reflux pump at last; The cat head working pressure of described iso-pentane tower is 630kPa-650kPa; The overhead vapours temperature is 95 ℃-100 ℃, is 95 ℃-100 ℃ through temperature behind the Skellysolve A tower reboiler, is 55 ℃-86 ℃ through temperature behind the reboiler of azeotrope column; Through temperature behind the condensate preheater is 50 ℃-80 ℃, and the temperature of the raw material after preheating is 45 ℃-75 ℃; The theoretical stage of described azeotrope column is 70-80; Working pressure 160kPa-180kPa, reflux ratio is 90-100,63 ℃-66 ℃ of tower top temperatures; And the mass ratio that its cat head neohexane and hexanaphthene take out is 1: 2.21～1: 2.23, and the vaporization rate of described Skellysolve A tower bottom reboiler is 0.25.
2. system that realizes the double-effect distillation method of the described hybrid pentane isomer fine separation of claim 1; It is characterized in that: it comprises condensate preheater, lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, the pentamethylene tower that discharge port and opening for feed link to each other through pipeline successively; The top of each tower all is connected with condensing surface and return tank, bottom all are connected with reboiler in described lightness-removing column, iso-pentane tower, Skellysolve A tower, azeotrope column, the pentamethylene tower; Link to each other through the feeding mouth of first outlet line at the bottom of the tower of described Skellysolve A tower with described azeotrope column middle part; The discharge port of described azeotrope column bottom links to each other with the feeding mouth at the middle part of described pentamethylene tower through second outlet line, and the cat head of described iso-pentane tower passes through reboiler, the condensate preheater of reboiler, the azeotrope column of the 3rd outlet line and Skellysolve A tower, the overhead condenser of iso-pentane tower links to each other successively.
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| CN102391063B (en) * | 2011-09-20 | 2013-12-11 | 中国石油天然气集团公司 | Process method and equipment for refining, extracting and distilling cyclopentane |
| CN103073376A (en) * | 2013-02-22 | 2013-05-01 | 南京炼油厂有限责任公司 | Separation process of mixed pentane |
| CN104725180A (en) * | 2015-02-12 | 2015-06-24 | 新疆独山子天利实业总公司 | Method for producing pentane foaming agent with different direct ratio of 3:7 |
| CN106478339B (en) * | 2015-08-26 | 2020-02-07 | 中国石油化工股份有限公司 | Method for separating cyclopentane and 2, 2-dimethylbutane |
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