CN103086833B - Method for separating C5 fraction - Google Patents
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- CN103086833B CN103086833B CN201110341429.3A CN201110341429A CN103086833B CN 103086833 B CN103086833 B CN 103086833B CN 201110341429 A CN201110341429 A CN 201110341429A CN 103086833 B CN103086833 B CN 103086833B
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Abstract
The invention discloses a method for separating C5 fraction. The method comprises the steps of pretreatment, extractive distillation, isoprene refining, piperylene refining, and dicyclopentadiene refining. During the isoprene refining process, isoprene is separated through azeotropic rectification, and azeotropic material flow is a product from an extractive distillation tower top. The flow rate ratio of the azeotropic material flow to the C5 removing tower top recovered material is 0.01-1. The two are mixed and are delivered into an isoprene tower. A plate number of the isoprene tower is 70-90. A reflux ratio is 15-25. With the method provided by the invention, isoprene product yield and purity can be improved, isoprene tower plate number and reflux ratio can be reduced, and equipment investment and operation cost can be reduced.
Description
Technical field
The present invention relates to organic chemical industry field, say further, relate to a kind of method of separating carbon 5 fraction, more particularly, is the method adopting azeotropic distillation, reactive distillation, extracting rectifying to carry out separating cracked carbon-5 fraction.
Background technology
Cracked C 5 fraction is the important joint product of ethylene producing device, and wherein isoprene (IP), cyclopentadiene (CPD) and m-pentadiene (PD) etc. are all the important source material of organic chemical industry and fine chemistry industry.Along with the development of petrochemical complex, separation and the utilization of cracked C 5 fraction are significant to the economy of ethylene unit of making rational use of resources, improve.
Existing C5 fraction separation process forms primarily of two-section extraction, and every section comprises extracting rectifying and stripping.C5 fraction is introduced into pretreatment unit, and pretreatment unit comprises pre-de-light, dimerization reaction, pre-de-heavy three parts.C5 fraction removes most of low boiling component in raw material pre-taking off in light packs putting, then dipolymer reactor is entered, be dicyclopentadiene (DCPD) at this most of cyclopentadiene, dimerisation products enters pre-de-refitting again and puts, and isoprene and m-pentadiene, dicyclopentadiene are carried out initial gross separation.Pre-weight-removing column tower top material enters the first extractive distillation column, extracting rectifying column overhead isolates alkane and monoolefine as raffinate, isoprene and solvent enter the first stripping tower, the C5 fraction that stripping goes out enters weight-removing column, is separated further with m-pentadiene, dicyclopentadiene at this isoprene.Thick isoprene enters the second extracting rectifying unit, remove a small amount of cyclopentadiene wherein and alkynes, the isoprene of the second extracting rectifying tower top enters that lightness-removing column is refining further obtains qualified polymerization grade isoprene product, the solvent of extracting rectifying tower reactor enters the second stripping tower below and vacuum stripper carries out stripping, and isolated solvent recycled utilizes.M-pentadiene and dicyclopentadiene refined unit is sent to from the material of pre-weight-removing column and weight-removing column still.Existing C5 fraction separation process is longer, and equipment number of units is many, complicated operation.
In order to improve existing C5 fraction separation process, each research unit has carried out large quantifier elimination, makes some progress.
Chinese patent CN1412165 discloses a kind of selective catalysis hydrogenation technique and removes alkynes, C 5 diene in five fractions of petroleum cracked carbon and other component are carried out the one-section abstraction rectification technique that is separated.Its feature is, before carbon five material carries out extracting and separating, first removes alkynes wherein by selective catalytic hydrogenation technique, then removes micro-cyclopentadiene through reactive distillation.This technique eliminates second segment extracting rectifying, simplifies solvent recovery unit, decreases investment cost, process cost and energy consumption, reduces production cost.But owing to have employed catalyzed reaction in process, quality product can be subject to the impact of the performance such as catalyst activity, selectivity, the production cycle also can be subject to the restriction of catalyst life.
Chinese patent CN1253130 discloses a kind of method adopting reactive distillation process separating diolefin from C5 fraction, while making cyclopentadiene generation dimerization reaction by reactive distillation, isoprene is separated by tower top, and material is again through rectifying separation m-pentadiene, dicyclopentadiene and isoprene.This invention adopts a reactive distillation column to replace dipolymer reactor of the prior art and pre-weight-removing column, and the working pressure of reactive distillation column is well below the pressure of dipolymer reactor, decreases facility investment.Have employed reactive distillation in this invention, dimerization reaction carries out in rectifying tower, but the residence time of cyclopentadiene in tower and reaction depth, transformation efficiency can by the impact of rectifying tower operation and restriction.
Chinese patent CN1490286 discloses a kind of method adopting reactive distillation and selective catalytic hydrogenation process integration to carry out separating cracked carbon-5 fraction.Pass through reactive distillation process, eliminate the hot dipolymer reactor usually adopted, alkynes is removed by selective catalytic hydrogenation technique, alkynes is removed before extracting rectifying, eliminate the second segment extracting rectifying usually adopted, shorten whole technical process, decrease facility investment and process cost, reduce production cost.Although the separation process of C5 fraction is simplified in this invention, but owing to have employed catalytic hydrogenation reaction and reaction rectification technique, the operational cycle that there is quality product and device equally limits by catalyst performance, the transforming degree of the dimerization of cyclopentadiene is subject to the problem of rectifying tower operating influence.
Chinese patent CN101244974 discloses a kind of method of one-section abstraction distillation separation cracking carbon 5-cut fraction, the method utilizes rectificating method remove cyclopentadiene and utilize azeotropic distillation method to remove alkynes, do not need reextraction just can obtain polymerization grade isoprene product, eliminate the second extraction cells and solvent treatment tower, the method is simple to operate, be easy to realize, production cost reduces.But the method only obtains isoprene product, m-pentadiene product separation unit is not improved.
In sum, existing technique also exists the problems such as flow process complexity, operational difficulty.
Summary of the invention
In order to solve, the flow process that in prior art, C5 fraction separating process exists is complicated, the problem of operational difficulty, the invention provides a kind of method of separating carbon 5 fraction, m-pentadiene product yield and purity can be improved, and decrease m-pentadiene stage number and reflux ratio, decrease facility investment and process cost.
The object of this invention is to provide a kind of method of separating carbon 5 fraction.
Comprise: pre-treatment, extracting rectifying, isoprene is refining, m-pentadiene refining and dicyclopentadiene is refined,
Adopt azeotropic distillation compartment pentadiene in described m-pentadiene treating process, azeotropic stream is from extracting rectifying tower top product;
Described m-pentadiene is refined and is carried out in m-pentadiene tower, and the stage number of m-pentadiene tower is 70 ~ 90, reflux ratio 15 ~ 25;
The flow of described azeotropic stream is 0.01 ~ 1 with the ratio of decarburization five column overhead extraction mass flow, enters m-pentadiene tower after the two mixing.
Azeotropic distillation, also known as sequence of constant boiling and rectification, is the rectifying that the character utilizing the component in mixture can form azeotrope realizes being separated.Usually in solution to be separated, add entrainer (or claiming entrainment agent), make one or two component in itself and solution form azeotrope, make separation be easy to carry out with the relative volatility increased between component to be separated.Yet there are no about forming the report of azeotrope with cyclopentadiene.
What adopt in existing m-pentadiene sepn process is the method for conventional distillation.Due to cyclopentadiene and trans-m-pentadiene boiling point closely, have to adopt high stage number to be separated with large reflux ratio.In m-pentadiene product separation flow process, also do not adopt the report of azeotropic distillation technology at present.
Contriver finds after deliberation, and cyclopentadiene and Skellysolve A can form azeotrope, azeotropic temperature 35.29 degree; Cyclopentadiene and 2-methyl-2-butene also can form azeotrope, azeotropic temperature 37.7 degree.Utilize them to form the principle of azeotropic, in the charging of m-pentadiene tower, introduce one logistics containing Skellysolve A and 2-methyl-2-butene, most of cyclopentadiene can be taken out of from m-pentadiene tower top, thus cyclopentadiene is removed.
Specifically comprise the following steps:
(1) pre-treatment: C5 fraction will be mixed and send into weight-removing column, carry out reactive distillation, lightness-removing column is sent into from overhead extraction light constituent, from weight-removing column still extraction heavy constituent, be sent to m-pentadiene and dicyclopentadiene refined unit, lightness-removing column adopts azeotropic distillation, and lightness-removing column still extraction material enters extractive distillation column;
(2) extracting rectifying: through extracting rectifying, kettle material sends into desorption tower, the extraction of tower top material parts, and part sends into m-pentadiene tower as azeotropic stream; The extraction of desorb tower reactor material parts, part returns extractive distillation column, and isoprene treating tower sent into by desorb tower top material;
(3) isoprene is refined: in isoprene treating tower, carry out reactive distillation, and tower reactor extraction heavy constituent sends into decarburization five tower;
(4) m-pentadiene and dicyclopentadiene are refined: decarburization five kettle material sends into dicyclopentadiene tower, m-pentadiene tower is entered after the azeotropic stream mixing of decarburization five column overhead extraction material and extractive distillation column overhead extraction, carry out azeotropic distillation, m-pentadiene column overhead material returns weight-removing column, m-pentadiene tower side take-off m-pentadiene product; Dicyclopentadiene tower side take-off dicyclopentadiene product.
Specifically can by the following technical solutions:
(1) pre-treatment: pretreatment unit comprises weight-removing column and lightness-removing column; To mix C5 fraction and send into weight-removing column, and adopt reaction rectification technique in this tower, cyclopentadiene generation dimerization reaction generates dicyclopentadiene, and cyclopentadiene transformation efficiency is more than 80%; Through being separated, comprise the light constituent of isoprene, alkane, monoolefine and a small amount of cyclopentadiene from overhead extraction; The heavy constituent comprising dicyclopentadiene and most m-pentadiene, from tower reactor extraction, is sent to m-pentadiene and dicyclopentadiene refined unit; Described alkane, monoolefine are pentane, amylene etc.; Described weight-removing column overhead stream is sent into lightness-removing column, lightness-removing column adopts azeotropic distillation technology, form the principle of azeotrope according to iso-pentane and carbon five alkynes, will comprise the light constituent of iso-pentane and alkynes from lightness-removing column overhead extraction, alkynes reaches more than 99% in the rate of recovery of tower top; Comprise isoprene, alkane, monoolefine and a small amount of cyclopentadiene, the material of m-pentadiene draws from tower reactor;
(2) extracting rectifying: lightness-removing column kettle material is introduced extractive distillation column, and carry out extracting rectifying in the presence of solvent, the Their Insoluble Components comprising alkane, monoolefine etc., from overhead extraction, is rich in the solvent material of isoprene from tower reactor extraction, sends into desorption tower; The solvent material being rich in isoprene obtained from extractive distillation column tower reactor is separated desorption tower, comprise isoprene and a small amount of cyclopentadiene, m-pentadiene material from overhead extraction, solvent, from tower reactor extraction, loops back extractive distillation column, and extraction section solvent send solvent regeneration unit;
(3) isoprene is refined: desorption tower tower top material is introduced isoprene treating tower, and this tower adopts reaction rectification technique, and the cyclopentadiene do not transformed completely continues that dimerization reaction occurs and generates dicyclopentadiene; The a small amount of thick isoprene of overhead extraction, near the side take-off isoprene product of tower top, the concentration controlling cyclopentadiene in product is less than 1ppm; Comprise m-pentadiene, dicyclopentadiene heavy constituent from tower reactor extraction, be sent to m-pentadiene and dicyclopentadiene refined unit;
(4) m-pentadiene and dicyclopentadiene are refined: m-pentadiene and dicyclopentadiene refined unit comprise decarburization five tower, m-pentadiene tower and dicyclopentadiene tower; Be incorporated into decarburization five tower after weight-removing column kettle material by step (1) being mixed with step (3) isoprene treating tower kettle material to be separated, this tower adopts reaction rectification technique, carbon five component that overhead extraction includes m-pentadiene is sent to m-pentadiene tower, and tower reactor extraction includes carbon six, the heavy constituent of dicyclopentadiene is sent to dicyclopentadiene tower; Decarburization five column overhead material and one is from the charging as m-pentadiene tower after the mixing of materials of extracting rectifying tower top, from extracting rectifying tower top material containing the component such as Skellysolve A, 2-methyl-2-butene; M-pentadiene tower adopts azeotropic distillation technology, and form the principle of azeotrope according to cyclopentadiene and Skellysolve A, cyclopentadiene and 2-methyl-2-butene, overhead extraction comprises the light constituents such as cyclopentadiene, Skellysolve A, 2-methyl-2-butene and returns weight-removing column; Near tower reactor side take-off m-pentadiene product, kettle material returns decarburization five tower; From the charging of decarburization five kettle material as dicyclopentadiene tower, near tower reactor side take-off dicyclopentadiene product, overhead extraction carbon six light constituent, part returns decarburization five tower tower reactor, all the other carrying devices.
In the method for the invention, to the number of theoretical plate of each rectifying tower and concrete operations condition, there is no particular limitation, those skilled in the art can select suitable number of theoretical plate and operational condition according to practical situation, can by changing number of theoretical plate, feed rate and reflux ratio reach each tower is separated object.For given logistics composition, under certain pressure, the boiling point of this logistics is determined, the determination of these parameters for a person skilled in the art, is easily.
List the preferred operating parameters of method of the present invention below:
In described step (1), the number of theoretical plate of preferred described weight-removing column is 55 ~ 75, and working pressure is 0.25 ~ 0.35MPa, tower top temperature is 65 ~ 75 DEG C, bottom temperature is 90 ~ 110 DEG C, and reflux ratio is 5 ~ 15, controls liquid at dwell time in the tower at 0.5 ~ 3.5 hour.
In described step (1), lower boiling carbon Four composition and iso-pentane, from overhead extraction, utilize iso-pentane and alkynes to form the principle of azeotrope, and most of alkynes also will with iso-pentane from overhead extraction, and the rate of recovery of tower top alkynes reaches more than 99%.For controlling isoprene in the loss amount of tower top and the alkynes rate of recovery at tower top, the operational condition of preferably described lightness-removing column is: number of theoretical plate 100 ~ 140, reflux ratio 10 ~ 20.
In described step (2), the number of theoretical plate of preferably described extractive distillation column is 70 ~ 120.Preferably described solvent enters described extractive distillation column from tower top 6 ~ 10 blocks of plates, and described solvent is 2 ~ 10 with the mass ratio of the material entering extractive distillation column.
In described step (3), cyclopentadiene generation dimerization reaction generates dicyclopentadiene, and cyclopentadiene transformation efficiency reaches more than 99%, and the concentration controlling cyclopentadiene in product is less than 1ppm, controls liquid at dwell time in the tower at 0.5 ~ 3.5 hour.
In described step (4), decarburization five tower adopts reaction rectification technique, and cyclopentadiene generation dimerization reaction generates dicyclopentadiene.
In described step (4), the stage number of preferably described m-pentadiene tower is 70 ~ 90, reflux ratio 15 ~ 25, the flow of azeotropic stream sets according to the amount of the cyclopentadiene in carbon five column overhead extraction material, then corresponding azeotropic stream flow is just large for the content height of cyclopentadiene, can determine as the case may be, in the present invention, preferably described is 0.01 ~ 1 from extracting rectifying tower top mass flow and the ratio of decarburization five column overhead extraction mass flow.
In the method for extracting distillation separation C five cut of the present invention, any extraction solvent that in prior art, C5 fraction separation process is conventional can be used, the solvent used in preferably described step (2) is selected from the one in N-Methyl pyrrolidone, acetonitrile, N-N-formyl morpholine N-, N-Methylimidazole, DMF.
The method of the invention has following characteristics:
(1) utilize iso-pentane and alkynes to form the principle of azeotrope, just the alkynes in C5 fraction was removed before extracting rectifying, thus eliminate two-stage extraction rectifying, decrease number of devices, therefore enormously simplify flow process, decrease facility investment;
(2) adopt reaction rectification technique in the present invention, carry out in tower while of making reaction and be separated, eliminate hot dipolymer reactor of the prior art, decrease facility investment;
(3) boiling point of cyclopentadiene is 40.46 DEG C, the boiling point of trans-m-pentadiene is 42.03 DEG C, boiling point between two components closely, sizable difficulty is brought to the separation of m-pentadiene, in order to reach separation object, have in prior art adopt high stage number and large reflux ratio; Adopt azeotropic distillation to remove Cyclopentadiene in the present invention, obtain m-pentadiene product, m-pentadiene yield and purity high, and decrease m-pentadiene stage number and reflux ratio, decrease facility investment and process cost;
(4) owing to eliminating two-stage extraction rectification cell in the present invention, decrease solvent usage quantity and amount of regeneration, thus decrease process cost, simplify solvent regeneration unit;
(5) in carbon five tripping device in order to ensure safety, need the concentration of alkynes in control device, in the present invention, namely alkynes be removed at de-light unit, thus greatly strengthen device operation safety and stability.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
Fig. 2 is the schematic flow sheet of comparative example separating carbon 5 fraction.
Description of reference numerals:
1 weight-removing column; 2 lightness-removing columns; 3 extractive distillation columns; 4 desorption towers; 5 treating towers; 6 decarburization five towers; 7 m-pentadiene towers; 8 dicyclopentadiene towers
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As shown in Figure 1, the method for separating carbon 5 fraction, comprises the following steps:
(1) de-heavy: carbon Wuyuan material (mainly consists of carbon 4 8.4%, pentane 11.6%, amylene 19.2, alkynes 0.2%, isoprene 21.4%, cyclopentadiene 17.2%, m-pentadiene 13.9%, carbon 6 8.1%) be sent to weight-removing column 1, weight-removing column number of theoretical plate 62, working pressure 0.3MPa, tower top temperature 68 DEG C, bottom temperature 102 DEG C, liquid residence time 2.3 hours; At this, cyclopentadiene generation dimerization reaction generates dicyclopentadiene, transformation efficiency 85%; The heavy constituent such as m-pentadiene, dicyclopentadiene is separated with isoprene, m-pentadiene and dicyclopentadiene refined unit is sent to from tower reactor extraction, m-pentadiene and dicyclopentadiene reach more than 99.5% in the rate of recovery of tower reactor, and the light constituents such as isoprene are sent to lightness-removing column 2 from overhead extraction;
(2) de-light: be admitted to lightness-removing column 2 from weight-removing column top material, the number of theoretical plate of lightness-removing column is 120, and operating reflux ratio is 16, and the light constituents such as carbon four, alkynes and iso-pentane are from overhead extraction, and lightness-removing column still material is sent to extractive distillation column 3; The content controlling lightness-removing column tower top isoprene is 1%, carbon 4 40.6%, iso-pentane 24.8%, alkynes 0.8%, and alkynes is 99% in the rate of recovery of tower top;
(3) extracting rectifying: solvent for use is DMF (N, dinethylformamide), solvent injects from extracting rectifying tower top the 10th block of plate, and spray C5 fraction, the theoretical value of extractive distillation column is 100, operational condition is: solvent ratio 6, tower top temperature 49.6 DEG C, tower top pressure 0.19MPa, reflux ratio 4, the Their Insoluble Components such as pentane, amylene from overhead extraction, is rich in the solvent of isoprene from tower reactor extraction as raffinate;
(4) desorb: the solvent being rich in isoprene is sent to desorption tower 4, and the hydro carbons such as isoprene are sent to isoprene treating tower 5 from overhead extraction, and solvent is sent to extractive distillation column recycle from tower reactor extraction, another extraction section desolventizing regeneration unit;
(5) isoprene is refined: desorption tower 4 pushes up material and is sent to isoprene treating tower 5, and at this, unreacted cyclopentadiene continues that dimerization reaction occurs and generates dicyclopentadiene, and cyclopentadiene transformation efficiency is 99%, and liquid was dwell time in the tower 2 hours; The heavy constituents such as isoprene and m-pentadiene, cyclopentadiene and dicyclopentadiene are separated, and obtain polymerization grade isoprene product at tower top side line, the heavy constituent of tower reactor is sent to m-pentadiene and dicyclopentadiene refined unit;
(6) m-pentadiene and dicyclopentadiene refined unit: from weight-removing column 1 kettle material be introduced in decarburization five tower 6 from treating tower 5 kettle material, liquid is 1.8 hours at dwell time in the tower, carbon five component that overhead extraction contains m-pentadiene is sent to m-pentadiene tower 7, tower reactor extraction contains the heavy constituent of carbon six, dicyclopentadiene, is sent to dicyclopentadiene tower 8; Be 0.1 from extracting rectifying tower top material and the ratio of decarburization five column overhead extraction mass flow, m-pentadiene tower is entered after the two mixing, m-pentadiene tower 7 has column plate 85 pieces, from the 30th piece of plate charging, tower top pressure 0.13MPa, tower top temperature 40 DEG C, tower reactor pressure 0.2MPa, bottom temperature 90 DEG C, reflux ratio 20.Tower body side line 82 pieces of plate extraction m-pentadiene products, trans-m-pentadiene 48.1%, m-pentadiene summation content 78%, wherein cyclopentadiene 0.2%; Dicyclopentadiene tower tower reactor side take-off dicyclopentadiene product.
Comparative example:
As shown in Figure 2, the method for separating carbon 5 fraction, comprises the following steps:
De-heavy, de-light, extracting rectifying, desorb, isoprene purification step are with embodiment 1;
M-pentadiene and dicyclopentadiene refined unit: from weight-removing column 1 kettle material be introduced in decarburization five tower 6 from treating tower 5 kettle material, decarburization five stage number 42, from 24 pieces of plate chargings, carbon five component that overhead extraction contains m-pentadiene is sent to m-pentadiene tower 7, tower reactor extraction contains the heavy constituent of carbon six, dicyclopentadiene, is sent to dicyclopentadiene tower 8; M-pentadiene column plate 100 pieces, from the 43rd piece of plate charging, tower top pressure 0.13MPa, tower top temperature 42 DEG C, tower reactor pressure 0.2MPa, bottom temperature 91 DEG C, reflux ratio 31.Tower body side line 95 pieces of plate extraction m-pentadiene products, trans-m-pentadiene 47.6%, cis-form m-pentadiene and trans summation content 70%, wherein cyclopentadiene 0.4%; Dicyclopentadiene tower tower reactor side take-off dicyclopentadiene product.
Contrast above result, adopt the inventive method compartment pentadiene product, reduce the stage number of m-pentadiene tower, reduce reflux ratio, improve product purity.
Claims (3)
1. a method for separating carbon 5 fraction, comprising: pre-treatment, extracting rectifying, isoprene is refining, m-pentadiene refining and dicyclopentadiene is refined, and it is characterized in that:
Adopt azeotropic distillation compartment pentadiene in described m-pentadiene treating process, azeotropic stream is from extracting rectifying tower top product;
(1) pre-treatment: C5 fraction will be mixed and send into weight-removing column, carry out reactive distillation, lightness-removing column is sent into from overhead extraction light constituent, from weight-removing column still extraction heavy constituent, be sent to m-pentadiene and dicyclopentadiene refined unit, lightness-removing column adopts azeotropic distillation, and lightness-removing column still extraction material enters extractive distillation column;
(2) extracting rectifying: through extracting rectifying, kettle material sends into desorption tower, the extraction of tower top material parts, and part sends into m-pentadiene tower as azeotropic stream; The extraction of desorb tower reactor material parts, part returns extractive distillation column, and isoprene treating tower sent into by desorb tower top material;
(3) isoprene is refined: in isoprene treating tower, carry out reactive distillation, and tower reactor extraction heavy constituent sends into decarburization five tower;
(4) m-pentadiene and dicyclopentadiene are refined: decarburization five kettle material sends into dicyclopentadiene tower, m-pentadiene tower is entered after the azeotropic stream mixing of decarburization five column overhead material and extractive distillation column overhead extraction, carry out azeotropic distillation, m-pentadiene column overhead material returns weight-removing column, m-pentadiene tower side take-off m-pentadiene product; Dicyclopentadiene tower side take-off dicyclopentadiene product.
2. the method for separating carbon 5 fraction as claimed in claim 1, is characterized in that:
Described m-pentadiene is refined and is carried out in m-pentadiene tower, and the stage number of m-pentadiene tower is 70 ~ 90, reflux ratio 15 ~ 25.
3. the method for separating carbon 5 fraction as claimed in claim 2, is characterized in that:
The flow of described azeotropic stream is 0.01 ~ 1 with the ratio of decarburization five column overhead extraction mass flow, enters m-pentadiene tower after the two mixing.
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| CN101244973B (en) * | 2007-02-15 | 2010-05-19 | 中国石油化工股份有限公司 | Method for removing alkyne in high purity isoprene |
| CN101244974B (en) * | 2007-02-15 | 2010-05-19 | 中国石油化工股份有限公司 | Method for one-section abstraction distillation separation cracking carbon 5-cut fraction |
| CN101302134B (en) * | 2007-05-11 | 2010-05-26 | 中国石油化工股份有限公司 | Method for separating cracked carbon-5 fraction by front-end alkyne removal one-stage extraction |
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