CN103183577A - Heat exchange system and heat exchange method for carbon five extractive distillation - Google Patents
Heat exchange system and heat exchange method for carbon five extractive distillation Download PDFInfo
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- CN103183577A CN103183577A CN2011104511642A CN201110451164A CN103183577A CN 103183577 A CN103183577 A CN 103183577A CN 2011104511642 A CN2011104511642 A CN 2011104511642A CN 201110451164 A CN201110451164 A CN 201110451164A CN 103183577 A CN103183577 A CN 103183577A
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Abstract
The invention discloses a heat exchange system and a heat exchange method for carbon five extractive distillation. The system comprises a first extraction tower divided into upper and lower sections, wherein the lower section of the first extraction tower is provided a lower section reboiler A; a de-heavy fractionator divided into upper and lower sections, wherein the upper section of the de-heavy fractionator is provided with an upper section reboiler A; and a second extraction tower into divided upper and lower sections provided with an upper section reboiler B and a lower section reboiler B respectively. The heat exchange method comprises the steps that materials at the bottom of a first stripping tower are exchanged heat through the lower section reboiler A and the upper section reboiler A of the de-heavy fractionator and sent to the upper section of the first extraction tower; materials at the bottom of a second stripping tower are exchanged heat through the lower section reboiler B and sent to the upper section of a third stripping tower; and materials at the bottom of the third stripping tower are exchanged heat through the upper section reboiler B, cooled and sent to a solvent feeding port at the upper section of the second extraction tower. The heat exchange system and the heat exchange method realize gradient recovery and utilization of energy, and have the advantages of low investment, low energy consumption, simple process route and the like in industrial applications.
Description
Technical field
The present invention relates to chemical field, say further, relate to a kind of heat-exchange system and heat-exchange method of carbon five extracting rectifyings.
Background technology
The C5 fraction of the quite a lot of quantity of by-product in the petroleum cracking process of producing ethylene, dienes such as isoprene, m-pentadiene and cyclopentadiene are rich in C5 fraction.These diolefin chemical property are active, are important chemical material.Because the difference on raw material, cracking severity and the separation degree of petroleum hydrocarbon cracking, the diolefin content in the C5 fraction is different, but total amount is in the middle of 40～60%.Therefore, separation utilizes C5 fraction to have profound significance for the economic benefit that improves ethylene unit, comprehensive utilization petroleum resources.
Cracked C 5 fraction is close by more than 20 kinds of boiling points, and the component that easily forms azeotrope is to each other formed, and the diolefin difficulty of therefrom isolating purity load application requiring is higher, and technology is comparatively complicated, generally adopts extraction fractional distillation in the prior art.Selective solvent commonly used has dimethyl formamide (DMF) and acetonitrile, as disclosed processing methodes such as patent JP63101338, JP74019245, US3510405, US3535260.Because the boiling point of extraction agent is higher than carbon five hydrocarbon far away, its heat enthalpy value is higher, if can carbon five plant energy consumptions further be reduced its reasonable utilization.Traditional process adopts a cover hot-water system to carry out the solvent heat exchange, but temperature influence heat exchange effect is limited, and the hot water of the steam condensate by-product of this device by-product is excessive simultaneously, and therefore, carbon five plant energy consumptions of traditional process are higher, directly influence the economic benefit of device.
Summary of the invention
For solving in the prior art in the problem aspect energy recovery and the UTILIZATION OF VESIDUAL HEAT IN, the invention provides a kind of heat-exchange system and heat-exchange method of carbon five extracting rectifyings, the step of having realized energy reclaims and utilization, has advantages such as reduced investment, energy consumption is low, operational path is simple and direct in industrial application.
One of purpose of the present invention provides a kind of heat-exchange system of carbon five extracting rectifyings.
Comprise: first extraction tower, first stripping tower, weight-removing column, second extraction tower, second stripping tower and the 3rd stripping tower, each Tata still is provided with reboiler, first extraction tower, second extraction tower and weight-removing column are divided into two sections respectively, the first extraction tower hypomere arranges hypomere reboiler A, described hypomere reboiler A is arranged on optional position between hypomere tower reactor the 1st to 10 block of plate reciprocal usually, the first extraction tower epimere is provided with the solvent feed mouth, and the first extraction tower hypomere is provided with carbon five opening for feeds;
Weight-removing column is divided into two sections, and the weight-removing column epimere arranges epimere reboiler A, and described epimere reboiler A is arranged on optional position between epimere tower reactor the 1st to 10 block of plate reciprocal;
After described first stripping tower tower reactor outlet connects the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A successively, connect the first extraction tower epimere solvent feed mouth; Also can the first stripping tower tower reactor after outlet connects the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A and a collection solvent cooler A successively, connect the first extraction tower epimere solvent feed mouth;
The described second extraction tower epimere and hypomere arrange epimere reboiler B and hypomere reboiler B respectively, and described epimere reboiler B is arranged on optional position between epimere tower reactor the 1st to 10 block of plate reciprocal; Described hypomere reboiler B is arranged on optional position between hypomere tower reactor the 1st to 10 block of plate reciprocal;
The second extraction tower epimere is provided with the solvent feed mouth; The second extraction tower hypomere is provided with weight-removing column top material opening for feed;
After described second stripping tower tower reactor outlet connects the second extraction tower hypomere reboiler B, connect the 3rd stripping tower;
The outlet of the 3rd stripping tower tower reactor connects the second extraction tower epimere solvent feed mouth after connecting the second extraction tower epimere reboiler B, two collection solvent cooler B successively.
Above-described first extraction tower, second extraction tower and weight-removing column are divided into two sections to be divided with stage number, and there is no particular limitation, and preferably stage number is divided into two sections.
Two of purpose of the present invention provides a kind of heat-exchange method of carbon five extracting rectifyings.
Comprise:
The first stripping tower tower reactor material after cooling off or without cooling, is sent into the first extraction tower epimere as solvent after the epimere reboiler A heat exchange of the hypomere reboiler A of first extraction tower and weight-removing column;
The second stripping tower tower reactor material is sent into the 3rd stripping tower top after the second extraction tower hypomere reboiler B heat exchange;
The 3rd stripping tower tower reactor material through cooling, is sent into the second extraction tower epimere solvent feed mouth after the second extraction tower epimere reboiler B heat exchange.
Wherein, first extraction tower and second extraction tower can adopt setting of the prior art and processing condition, can be preferred among the present invention:
The total stage number of described first extraction tower is 100～200, and working pressure is 0.03～0.2MPaG, and tower top temperature is 35～60 ℃, and 100～140 ℃ of tower reactor temperature, reflux ratio are 1～5, and solvent ratio is 1～10;
The total stage number of described second extraction tower is 100～200, and working pressure is 0.03～0.2MPaG, and tower top temperature is 35～60 ℃, and 100～140 ℃ of tower reactor temperature, reflux ratio are 1～5, and solvent ratio is 1～10.
Described first extraction tower and the second extraction tower column internals adopt sieve plate, float valve or their composite type.
Setting and the processing condition of first stripping tower among the present invention, weight-removing column, second stripping tower, the 3rd stripping tower can adopt setting of the prior art and processing condition.
The present invention can be achieved through the following technical solutions:
First extraction tower is divided into two sections, and the top of epimere 1A arranges the opening for feed of extraction solvent, and hypomere 1B top arranges carbon five feeding lines, and hypomere tower bottom arranges hypomere reboiler A, and hypomere tower reactor extraction pipeline links to each other with the first stripping tower feeding line; First stripper overhead stream is divided two strands after condensation, one sends into the first extraction tower tower reactor reboiler entrance, another thigh is sent into the weight-removing column hypomere, the first stripping tower tower reactor extraction lean solvent is after the hypomere reboiler A of first extraction tower heat exchange, then through the epimere reboiler A of weight-removing column heat exchange, after water cooler A cooling or without cooling, directly link to each other with the first extraction tower epimere 1A as the solvent feed of first extraction tower again; By weight-removing column epimere 3A cat head production flow through the cooling after send into the second extraction tower hypomere 4A top, m-pentadiene is then sent in tower reactor extraction logistics, the dicyclopentadiene processing unit; Second extraction tower is divided into two sections, the top of epimere 4A arranges the lean solvent feeding line, the second extraction tower epimere 4A tower reactor arranges epimere reboiler B, hypomere 4B top arranges carbon five feeding lines, hypomere 4B bottom arranges hypomere reboiler B, and hypomere tower reactor extraction pipeline links to each other with the second stripping tower feeding line; Second stripper overhead stream is divided two strands after condensation, one sends into the second extraction tower tower reactor reboiler entrance, another burst extraction, the second stripping tower reactor extraction lean solvent through the hypomere reboiler B heat exchange of second extraction tower after as the 3rd stripping tower charging; The 3rd stripping tower tower reactor extraction lean solvent through the second extraction tower epimere reboiler B heat exchange after, the solvent feed as second extraction tower after water cooler B cooling links to each other with the second extraction tower epimere 4A.
Heat-exchange method of the present invention is: be the thermal source of the first extraction tower epimere reboiler A as hypomere reboiler A, the weight-removing column of first extraction tower successively with the lean solvent of the first stripping tower reactor extraction, sending into first extraction tower again after water cooler A cooling after the heat exchange recycles as solvent feed, or directly send into first extraction tower without water cooler and recycle as solvent feed, decide on circulating solvent temperature out after the heat exchange of weight-removing column epimere tower reactor reboiler;
Send into the 3rd stripping tower charging after the hypomere reboiler B thermal source heat exchange of lean solvent as second extraction tower by the second stripping tower reactor extraction; Sending into second extraction tower after the lean solvent of the 3rd stripping tower reactor extraction is lowered the temperature by water cooler B as the epimere reboiler B thermal source heat exchange of second extraction tower recycles as solvent feed.
Particularly,
Carbon five materials of being sent here by pretreatment unit enter the first extraction tower hypomere top, this tower is divided into hypomere, total stage number 100～200, working pressure is 0.03～0.2MPaG, 35～60 ℃ of tower top temperatures, reflux ratio 1～5, solvent ratio 1～10, column internals adopts sieve plate, float valve or their composite type; The first extraction cat head steams C 5 alkane, monoolefine, tower reactor extraction C 5 diene, alkynes and solvent; The first extraction tower hypomere (1B) arranges hypomere reboiler A from tower reactor the 1st to 10 plate optional position reciprocal, and heating medium is the lean solvent of the first stripping tower reactor extraction; The first extraction tower reactor production material is sent into first stripping tower and is separated, after hydrocarbon and separated from solvent, the solvent of the first stripping tower reactor reclaims through the epimere reboiler A of the hypomere reboiler A of first extraction tower and weight-removing column and sends into first extraction tower after heat is cooled to assigned temperature by water cooler A and recycle as solvent feed, or directly send into first extraction tower without water cooler A and recycle as solvent feed, decide on circulating solvent temperature out after the heat exchange of weight-removing column epimere tower reactor reboiler.
Carbon five materials of being sent here by the weight-removing column top enter the second extraction tower hypomere top, this tower is divided into hypomere, total stage number 100～200, working pressure is 0.03～0.2MPaG, 35～60 ℃ of tower top temperatures, reflux ratio 1～5, solvent ratio 1～10, column internals can adopt sieve plate, float valve or their composite type; The second extraction cat head steams the isoprene more than 99%, sends to lightness-removing column and further handles, tower reactor extraction C 5 diene, alkynes and solvent; The second extraction tower hypomere 4B arranges hypomere reboiler B from tower reactor the 1st to 10 plate optional position reciprocal, and heating medium is the lean solvent of the second stripping tower reactor extraction; The second extraction tower epimere 4A tower reactor arranges epimere reboiler B, and heating medium is the lean solvent of the 3rd stripping tower reactor extraction; The second extraction tower reactor production material is sent into second stripping tower and is carried out solvent recuperation, after removing alkynes, sends into the 3rd stripping tower charging after the hypomere reboiler B thermal source heat exchange of lean solvent as second extraction tower by the second stripping tower reactor extraction; Sending into second extraction tower after the lean solvent of the 3rd stripping tower reactor extraction is lowered the temperature by water cooler B as the epimere reboiler B thermal source heat exchange of second extraction tower recycles as solvent feed.
The present invention is used for solvent in the abstraction distillation system and is selected from least a in dimethyl formamide, N,N-DIMETHYLACETAMIDE, the N-Methyl pyrrolidone aqueous solution and the acetonitrile solution.
The present invention has the following advantages: 1. hot solvent has been realized cascaded utilization of energy, saves steam consumption 5～10%; 2. because the energy supplement of intermediate reboiler has reduced the especially vapour-liquid phase load of hypomere of tower, the gas phase load reduces 10～30%, and the liquid phase load reduces 1～10%, and the tower for taking as the leading factor with the gas phase load has dwindled tower diameter accordingly, has saved investment.
Description of drawings
Fig. 1 embodiments of the invention heat-exchange system schematic flow sheet
Fig. 2 Comparative Examples heat-exchange system schematic flow sheet
Description of reference numerals:
1-first extraction tower (A-epimere, B-hypomere), 2-first stripping tower, 3-weight-removing column (A-epimere, the B-hypomere), 4-second extraction tower (A-epimere, B-hypomere), 5-second stripping tower, 6-the 3rd stripping tower, the 7-first extraction tower tower reactor reboiler, the 8-first extraction tower hypomere reboiler A, the 9-first extraction tower epimere reboiler A, 10-one collection solvent cooler A, 11-first stripper reboiler, the 12-first stripping tower condenser, 13-weight-removing column reboiler, 14-weight-removing column condenser, the 15-second extraction tower tower reactor reboiler, the 16-second extraction tower hypomere reboiler B, the 17-second extraction tower epimere reboiler B, 18-two collection solvent cooler B, 19-second stripper reboiler, the 20-second stripping tower condenser, 21-the 3rd stripper reboiler, the 22-hot water heat exchanger
Embodiment
Below in conjunction with embodiment, further specify the present invention.
Embodiment:
As shown in Figure 1, a kind of heat-exchange system of carbon five extracting rectifyings.
Comprise: first extraction tower 1, first stripping tower 2, weight-removing column 3, second extraction tower 4, second stripping tower 5 and the 3rd stripping tower 6, each Tata still is provided with reboiler,
Described first extraction tower 1 is divided into two sections, and the first extraction tower hypomere arranges hypomere reboiler A8, and described hypomere reboiler A8 is arranged on from hypomere tower reactor the 2nd Board position reciprocal; First extraction tower, 1 epimere is provided with the solvent feed mouth, and first extraction tower, 1 hypomere is provided with carbon Wuyuan material opening for feed;
Weight-removing column 3 is divided into two sections, and the weight-removing column epimere arranges epimere reboiler A9, and described epimere reboiler A9 is arranged on from epimere tower reactor the 1st Board position reciprocal;
After the outlet of first stripping tower, 2 tower reactors connects hypomere reboiler A8, epimere reboiler A9 and water cooler A10 successively, connect first extraction tower, 1 epimere solvent feed mouth;
Described second extraction tower 4 is divided into two sections, and epimere reboiler B17 and hypomere reboiler B16 are set respectively; Described hypomere reboiler B16 is arranged on from hypomere tower reactor the 2nd Board position reciprocal, and described epimere reboiler B17 is arranged on from epimere tower reactor the 1st Board position reciprocal.
Second extraction tower, 4 epimeres are provided with the solvent feed mouth; Second extraction tower, 4 hypomeres are provided with weight-removing column top material opening for feed;
After described second stripping tower, 5 tower reactors outlet connects hypomere reboiler B16, connect the 3rd stripping tower 6;
After the outlet of the 3rd stripping tower 6 tower reactors connects epimere reboiler B17, water cooler B18 successively, connect second extraction tower, 4 epimere solvent feed mouths.
When carrying out heat exchange,
The first stripping tower tower reactor material after cooling, is sent into the first extraction tower epimere as solvent after the epimere reboiler A heat exchange of the hypomere reboiler A of first extraction tower and weight-removing column;
The second stripping tower tower reactor material is sent into the 3rd stripping tower top after the second extraction tower hypomere reboiler B heat exchange;
The 3rd stripping tower tower reactor material through cooling, is sent into the second extraction tower epimere solvent feed mouth as solvent after the second extraction Tata epimere reboiler B heat exchange.
Wherein, the total stage number of described first extraction tower is 149,77 blocks of plates of epimere wherein, 72 blocks of plates of hypomere, epimere cat head working pressure is 0.042MPaG, the epimere tower top temperature is 45 ℃, and reflux ratio is 3.5, and hypomere cat head working pressure is 0.082MPaG, 72 ℃ of hypomere tower top temperatures, 110 ℃ of hypomere tower reactor temperature, solvent ratio are 5 (solvent ratio is defined as the ratio of solvent feed amount and extraction tower carbon five inlet amounies, down with);
The total stage number of described second extraction tower is 186, wherein epimere is 94,92 of hypomeres, epimere cat head working pressure is 0.032MPaG, and the epimere tower top temperature is 42 ℃, and reflux ratio is 2, hypomere cat head working pressure is 0.082MPaG, 72 ℃ of hypomere tower top temperatures, 120 ℃ of hypomere tower reactor temperature, solvent ratio are 5;
Described first extraction tower and the second extraction tower column internals adopt valve tray.
Comparative Examples:
As shown in Figure 2, a kind of heat-exchange system of carbon five extracting rectifyings.
Comprise: first extraction tower 1, first stripping tower 2, weight-removing column 3, second extraction tower 4, second stripping tower 5 and the 3rd stripping tower 6, each Tata still is provided with reboiler,
Described first extraction tower 1 is divided into two sections, and the first extraction tower hypomere arranges hypomere reboiler A8, and described hypomere reboiler A8 is arranged on from tower reactor the 2nd Board position reciprocal; First extraction tower, 1 epimere is provided with the solvent feed mouth, and first extraction tower, 1 hypomere is provided with material inlet;
The outlet of first stripping tower, 2 tower reactors connects first extraction tower, 1 epimere solvent feed mouth after connecting hypomere reboiler A8, a collection solvent cooler A10 successively;
Described weight-removing column 3 is divided into two sections, and tower reactor has only a reboiler 13;
Described second extraction tower 4 is divided into two sections, wherein has only the hypomere tower reactor that a reboiler 15 is arranged;
Second extraction tower, 4 epimeres are provided with the solvent feed mouth; Second extraction tower, 4 hypomeres are provided with weight-removing column top material opening for feed;
After described second stripping tower, 5 tower reactors outlet connects hot water heat exchanger 22, connect the 3rd stripping tower 6;
The outlet of the 3rd stripping tower 6 tower reactors connects second extraction tower, 4 epimere solvent feed mouths after connecting two collection solvent cooler 18.
When carrying out heat exchange,
The first stripping tower tower reactor material after a collection solvent cooler 10 coolings, is sent into the first extraction tower epimere as solvent after the hypomere reboiler A8 of first extraction tower heat exchange;
The second stripping tower tower reactor material is sent into the 3rd stripping tower top after hot water heat exchanger 16 heat exchange;
The 3rd stripping tower tower reactor material is sent into the second extraction tower epimere solvent feed mouth through after 18 coolings of two collection solvent cooler.
Wherein, the total stage number of described first extraction tower is 149,77 blocks of plates of epimere wherein, 72 blocks of plates of hypomere, epimere cat head working pressure is 0.042MPaG, the epimere tower top temperature is 45 ℃, and reflux ratio is 3.5, and hypomere cat head working pressure is 0.082MPaG, 72 ℃ of hypomere tower top temperatures, 110 ℃ of hypomere tower reactor temperature, solvent ratio are 5 (solvent ratio is defined as the ratio of solvent feed amount and extraction tower carbon five inlet amounies, down with);
The total stage number of described second extraction tower is 186, wherein epimere is 94,92 of hypomeres, upper end cat head working pressure is 0.032MPaG, and the epimere tower top temperature is 42 ℃, and reflux ratio is 2, hypomere cat head working pressure is 0.082MPaG, 72 ℃ of hypomere tower top temperatures, 120 ℃ of hypomere tower reactor temperature, solvent ratio are 5;
Described first extraction tower and the second extraction tower column internals adopt valve tray.
Table 1 is the energy consumption contrast of embodiment and Comparative Examples.
Table 1
| Project | Comparative Examples | Embodiment | Deviation, % |
| The low-pressure steam consumption, t/hr | 47.67 | 43.84 | -8 |
| The middle pressure steam consumption, t/hr | 9.77 | 9.77 | 0 |
| Consumption of cooling-water, t/hr | 4449 | 4433 | -16 |
Data from table 1 adopt heat-exchange system of the present invention and heat-exchange method can obviously reduce steam consumption and cooling water consumption as can be seen, and are of the present invention remarkably productive thus, can obviously cut down the consumption of energy.
Claims (8)
1. the heat-exchange system of carbon five extracting rectifyings, comprise: first extraction tower, first stripping tower, weight-removing column, second extraction tower, second stripping tower and the 3rd stripping tower, each Tata still is provided with reboiler, first extraction tower, second extraction tower and weight-removing column are divided into two sections respectively, the first extraction tower hypomere arranges hypomere reboiler A, the first extraction tower epimere is provided with the solvent feed mouth, and the first extraction tower hypomere is provided with carbon five opening for feeds; It is characterized in that:
Described weight-removing column epimere arranges epimere reboiler A, and described epimere reboiler A is arranged on optional position between epimere tower reactor the 1st to 10 block of plate reciprocal;
After described first stripping tower tower reactor outlet connects the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A successively, connect the first extraction tower epimere solvent feed mouth.
2. the heat-exchange system of carbon five extracting rectifyings as claimed in claim 1 is characterized in that:
Described first stripping tower tower reactor outlet connects the first extraction tower epimere solvent feed mouth after connecting the first extraction tower hypomere reboiler A, weight-removing column epimere reboiler A and a collection solvent cooler A successively.
3. the heat-exchange system of carbon five extracting rectifyings as claimed in claim 1 is characterized in that:
The described second extraction tower epimere and hypomere arrange epimere reboiler B and hypomere reboiler B respectively; Described epimere reboiler B is arranged on optional position between epimere tower reactor the 1st to 10 block of plate reciprocal; Hypomere reboiler B is arranged on optional position between hypomere tower reactor the 1st to 10 block of plate reciprocal;
The second extraction tower epimere is provided with the solvent feed mouth; The second extraction tower hypomere is provided with weight-removing column top material opening for feed;
After described second stripping tower tower reactor outlet connects the second extraction tower hypomere reboiler B, connect the 3rd stripping tower;
The outlet of the 3rd stripping tower tower reactor connects the second extraction tower epimere solvent feed mouth after connecting the second extraction tower epimere reboiler B, two collection solvent cooler B successively.
4. the heat-exchange method of the heat-exchange system of described carbon five extracting rectifyings of one of an employing such as claim 1～3 comprises:
The first stripping tower tower reactor material is sent into the first extraction tower epimere after the epimere reboiler A heat exchange of the hypomere reboiler A of first extraction tower and weight-removing column.
5. heat-exchange method as claimed in claim 4 is characterized in that:
The first stripping tower tower reactor material is sent into the first extraction tower epimere as solvent again after cooling off after the epimere reboiler A heat exchange of the hypomere reboiler A of first extraction tower and weight-removing column.
6. heat-exchange method as claimed in claim 4 is characterized in that:
The second stripping tower tower reactor material is sent into the 3rd stripping tower top after the second extraction tower hypomere reboiler B heat exchange;
The 3rd stripping tower tower reactor material through cooling, is sent into the second extraction tower epimere solvent feed mouth after the second extraction Tata epimere reboiler B heat exchange.
7. as the described heat-exchange method of one of claim 4～6, it is characterized in that:
The total stage number of described first extraction tower is 100～200, and working pressure is 0.03～0.2MPaG, and tower top temperature is 35～60 ℃, and 100～140 ℃ of tower reactor temperature, reflux ratio are 1～5, and solvent ratio is 1～10.
8. heat-exchange method as claimed in claim 7 is characterized in that:
The total stage number of described second extraction tower is 100～200, and working pressure is 0.03～0.2MPaG, and tower top temperature is 35～60 ℃, and 100～140 ℃ of tower reactor temperature, reflux ratio are 1～5, and solvent ratio is 1～10.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103845914A (en) * | 2013-10-12 | 2014-06-11 | 洛阳瑞泽石化工程有限公司 | Arrangement method of double reboilers as well as double-reboiler equipment |
| CN106278782A (en) * | 2015-05-29 | 2017-01-04 | 汪上晓 | Carbon five product segregation apparatus |
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| CN101244974A (en) * | 2007-02-15 | 2008-08-20 | 中国石油化工股份有限公司 | Method for one-section abstraction distillation separation cracking carbon 5-cut fraction |
| CN101450885A (en) * | 2007-12-07 | 2009-06-10 | 中国石油化工股份有限公司 | Method for separating carbon 5 fraction by one-stage extraction and rectification |
| CN101723788A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Separation method of cracking C5 fractions |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101244974A (en) * | 2007-02-15 | 2008-08-20 | 中国石油化工股份有限公司 | Method for one-section abstraction distillation separation cracking carbon 5-cut fraction |
| CN101450885A (en) * | 2007-12-07 | 2009-06-10 | 中国石油化工股份有限公司 | Method for separating carbon 5 fraction by one-stage extraction and rectification |
| CN101723788A (en) * | 2008-10-10 | 2010-06-09 | 中国石油化工股份有限公司 | Separation method of cracking C5 fractions |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103845914A (en) * | 2013-10-12 | 2014-06-11 | 洛阳瑞泽石化工程有限公司 | Arrangement method of double reboilers as well as double-reboiler equipment |
| CN103845914B (en) * | 2013-10-12 | 2015-05-20 | 洛阳瑞泽石化工程有限公司 | Arrangement method of double reboilers as well as double-reboiler equipment |
| CN106278782A (en) * | 2015-05-29 | 2017-01-04 | 汪上晓 | Carbon five product segregation apparatus |
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Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: China Petrochemical Group Co., Ltd Patentee after: Sinopec Engineering Construction Co., Ltd Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: China Petrochemical Corp Patentee before: Sinopec Engineering Construction Co., Ltd |