CN101508624B - Method for separating and cracking cyclopentadienyl from carbon 5 fraction by reaction distillation - Google Patents
Method for separating and cracking cyclopentadienyl from carbon 5 fraction by reaction distillation Download PDFInfo
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- CN101508624B CN101508624B CN2008100577456A CN200810057745A CN101508624B CN 101508624 B CN101508624 B CN 101508624B CN 2008100577456 A CN2008100577456 A CN 2008100577456A CN 200810057745 A CN200810057745 A CN 200810057745A CN 101508624 B CN101508624 B CN 101508624B
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Abstract
The invention discloses a method for separating cyclopentadiene by reaction rectification, belongs to a separation method of cracking C5 fraction, solves the problem of secondary dimerization reaction for generating X3 and X2 in the prior thermal dimerization method for separating cyclopentadiene, and provides a method for separating cyclopentadiene from cracking C5 fraction by reaction rectification method. The method comprises steps of sending the cracking C5 fraction into the middle part of a reaction rectification tower, taking out fluid containing isoprene from the top of the tower through a reaction rectification process, and taking out fluid containing pentadiene, cyclopentadiene and dicyclopentadiene from the tower bottom. The method reduces the yield of X3 and the loss rate of isoprene. The method can reduce the amount of cyclopentadiene entering an extracting unit, coking amount of an extracting and rectifying unit and regenerating amount of solvent in the process of separating cyclopentadiene from cracking C5 fraction.
Description
Technical field
The present invention relates to a kind of separation method of cracked C 5 fraction, more particularly, the present invention relates to a kind of method that adopts reaction rectification technique separating ring pentadiene.
Background technology
Diolefins such as isoprene, cyclopentadiene and m-pentadiene are rich in a considerable amount of C5 fractions of by-product in the C5 fraction in the process of petroleum cracking system ethene.These diolefin chemical property are active, are important chemical material.Because petroleum hydrocarbon cracking raw materials, cracking severity and separation degree is different, diolefin content is different in the cracked C 5 fraction, and total content is between 40%～60%.Therefore, separate and utilize C5 fraction to improving the economic benefit of ethylene unit, the comprehensive utilization petroleum resources have far reaching significance.
Cracked C 5 fraction contain more than 20 kind of boiling point close, easily form the component of azeotrope each other, from wherein isolating the higher C 5 diene of comprehensive utilization value, technology is comparatively complicated.C5 fraction contains for example alkynes such as crotonylene and valylene, these alkynes content are generally in 0.1～2% scope, because their chemical property is active, be the main detrimental impurity of reaction of C 5 diene product and polymerization process, therefore the alkynes that removes effectively wherein is the important step of cracked C 5 fraction separating technology.
At present industrial from cracked C 5 fraction the separating ring pentadiene produce the dicyclopentadiene product and all adopt hot process for dimerization, make cracked C 5 fraction under the temperature of 80～130 ℃ of temperature ranges, carry out hot dimerization reaction, then through separating the dicyclopentadiene product that obtains certain purity.In this hot dimerization, the dimerization reaction of isoprene and cyclopentadiene, m-pentadiene and cyclopentadiene, isoprene self, m-pentadiene self etc. takes place inevitably, thereby generate dimers such as unwanted X3 and X2, influence isoprene yield and dicyclopentadiene product purity.X3 is meant the dimer of isoprene and cyclopentadiene, m-pentadiene and cyclopentadiene, and X2 is meant the dimer of isoprene self and the dimer of m-pentadiene self.
In CN 98124390.8, also propose in reaction fractionating tower, to carry out reactive distillation, but had many problems.For example, the stage number that provides reaction fractionating tower is 50～120, reflux ratio is 20～80, this reflux ratio is too big, cause the diameter of tower too big, energy consumption is too big, and fatal is that so big reflux ratio will make isoprene circulate repeatedly at rectifying section, thereby produce more dimer X2, X3, do not reach reactive distillation and reduce these dimeric purposes.So big reflux ratio illustrates that also the residence time of material on every block of column plate is shorter, make cyclopentadiene not be able to do in time or rare dimerization reaction just is tending towards flowing to the tower still, mainly be to rely on to separate isoprene and cyclopentadiene are separated, rather than with reacting promotion rectifying, like this, cyclopentadiene content is higher in the logistics of tower still extraction, still needs to carry out dimerization reaction.
Therefore, there is the secondary dimerization reaction that generates X3 and X2 and influences the isolating problem of cyclopentadiene in the present cracked C 5 fraction separation industries.
Summary of the invention
The present invention is directed in the present cracked C 5 fraction separation industries and to have the secondary dimerization reaction that generates X3 and X2 and to influence the isolating problem of cyclopentadiene, proposed to adopt the method for reactive distillation separating ring pentadiene from cracked C 5 fraction.
Concrete technical scheme is as follows:
The method of reactive distillation separating ring pentadiene of the present invention, comprise: cracked C 5 fraction is sent into the reaction fractionating tower middle part, comprise the logistics of isoprene from the cat head extraction through reactive distillation processes, comprise the logistics of m-pentadiene, cyclopentadiene and dicyclopentadiene from the extraction of tower still, described reaction fractionating tower is a plate distillation column, have 70～160 number of theoretical plates, reflux ratio is 5～15, tower top temperature is 40～60 ℃, and described reactive distillation processes is meant that in rectifying initial ring pentadiene dimerization becomes the process of the reaction of dicyclopentadiene.
Preferably, the design residence time of every block of column plate on the top 1/3～1/2 of described reaction fractionating tower is 5～15 seconds, and the design residence time of every block of column plate of bottom 2/3～1/2 is 10～25 seconds.
Preferred described method further comprises step: the logistics of reaction fractionating tower still extraction is entered decarburization five towers, comprise the logistics of carbon five hydrocarbon from decarburization five column overhead extraction through rectifying or reactive distillation processes, enter the dicyclopentadiene treating tower from the logistics of decarburization five Tata still extraction, obtain the dicyclopentadiene product through rectifying.
Preferred described method further comprises step: the logistics that comprises carbon five hydrocarbon of decarburization five column overhead extraction enters the m-pentadiene treating tower, makes with extra care Tata still or bottom side line extraction m-pentadiene product through rectifying from m-pentadiene.
Further preferred described decarburization five towers have 40～100 number of theoretical plates, and reflux ratio is 5～20, and tower top temperature is 40～60 ℃.
Described dicyclopentadiene treating tower and m-pentadiene treating tower can adopt existing full scale plant and industrial condition, therefore, and no longer auspicious here stating.
Method of the present invention can be applied in the device of production dicyclopentadiene product, also can be applied in the device of separating isoprene product.
When method of the present invention is applied in the flow process of extracting rectifying separating isoprene, enter pre-lightness-removing column from the logistics that comprises isoprene of described reactive distillation column overhead extraction, isolate the logistics that comprises carbon four and alkynes from cat head through rectifying, from the logistics of tower still extraction based on isoprene, described logistics based on isoprene enters isoprene extracting rectifying unit.
Preferred described pre-lightness-removing column has 60～120 number of theoretical plates, and reflux ratio is 5～30, and tower top temperature is 40～60 ℃.
Described isoprene extracting rectifying unit is two-section extraction rectification cell or one-section abstraction rectification cell, and described one-section abstraction rectification cell may further comprise the steps:
(1) described logistics based on isoprene enters the extraction tower middle part, extraction solvent enters from extraction tower top, through the extracting rectifying process, the raffinate that comprises C 5 alkane and monoolefine from the extraction of extraction tower cat head, enter Analytic Tower from the logistics of tower still extraction, from the isoprene logistics of Analytic Tower cat head extraction based on isoprene, the logistics of resolving the extraction of Tata still loops back extraction tower through resolving;
(2) enter the weight-removing column middle part from the isoprene logistics of Analytic Tower cat head extraction, through rectifying or reactive distillation processes from weight-removing column cat head extraction isoprene product, from weight-removing column tower still extraction heavy constituent.
Be meant the material that comprises m-pentadiene, cyclopentadiene, dicyclopentadiene, X3, X2 from the heavy constituent of weight-removing column tower still extraction.
Described two-section extraction rectification cell can be the two-section extraction rectification cell of present industrial use.Described one-section abstraction rectification cell also can propose the one-section abstraction separating unit in Chinese patent the 01136383.5th and No. 02131463.2.
Preferred described weight-removing column has 80～180 number of theoretical plates, and reflux ratio is 10～30, and tower top temperature is 40～60 ℃.
Described extraction solvent can be suitable for any solvent, for example is dimethyl formamide, acetonitrile or N-Methyl pyrrolidone.
In the present invention, there is no particular limitation to each reaction fractionating tower and Rectification Column's Theoretical Plate Number and concrete operations condition, those skilled in the art can select suitable number of theoretical plate and operational condition according to practical situation, can be by changing the purpose of separating that number of theoretical plate, feed rate and backflow recently reach each tower.Form for given logistics, the boiling point of this logistics is determined under the certain pressure, therefore can change temperature by changing pressure, and for example tower top temperature and tower still temperature etc. are to satisfy demand of practical production.
Of the present invention from the method for cracked C 5 fraction separating ring pentadiene, utilized the principle of reactive distillation fully, cyclopentadiene generation dimerization reaction generates dicyclopentadiene in above-mentioned reaction fractionating tower, because the relative volatility of dicyclopentadiene is less, thereby more be tending towards moving to the tower still, utilize reaction to promote rectifying thereby reach, simultaneously because the dicyclopentadiene that generates is constantly shifted to the tower still, thereby more help constantly carrying out of cyclopentadiene dimerization reaction, can avoid cyclopentadiene and isoprene effectively, m-pentadiene react generation dimer, the i.e. alleged X3 of those skilled in the art.Help reducing the loss of isoprene, m-pentadiene like this, improve the quality and the color of m-pentadiene product, dicyclopentadiene product.Yet in existing still formula or tubular type dipolymer reactor, the dicyclopentadiene that the cyclopentadiene dimerization reaction generates can not be removed in time, under certain temperature and pressure, cyclopentadiene and dicyclopentadiene are tending towards reaching chemical equilibrium, cyclopentadiene can not be reduced to very low degree, cyclopentadiene and isoprene, m-pentadiene generation dimerization reaction generate X3, cause isoprene, m-pentadiene loss, the quality variation of m-pentadiene product and dicyclopentadiene product.Industrial production is verified, and the generation of X3 is mainly derived from the dimerization reaction process.
In the method for the invention, dipolymer reactor has been omitted in the effect that makes full use of reactive distillation, thereby has overcome the drawback that industrial production exists.In the present invention, utilize reaction fractionating tower that the cyclopentadiene dimerization in the raw material is become dicyclopentadiene, isolate isoprene at this cat head, and isolate cyclopentadiene and dicyclopentadiene at the tower still, isoprene and cyclopentadiene are concentrated in the upper and lower of tower respectively, reduce contacting of isoprene and cyclopentadiene so as much as possible, thereby reduced the generation of X3.Thereby this tower both utilized dicyclopentadiene heavier be easy to the tower still move with promote cyclopentadiene from dimerization, utilizing refinery distillation to make isoprene and cyclopentadiene have different bodies of the tower again distributes, thereby reduced the reaction of isoprene and cyclopentadiene faster of codimerization speed, thereby reduced the X3 growing amount, reduced the isoprene rate of loss.Because this reaction fractionating tower has higher separating effect, make the cyclopentadiene amount of cat head reduce, thereby reduced unitary coking of extracting rectifying and solvent reclamation amount.
In order to make a large amount of cyclopentadiene dimerization in this tower become dicyclopentadiene and other dimer less, need to select comparatively suitable plate distillation column of the residence time, select for use suitable reflux ratio that cyclopentadiene is concentrated to promote dimerization reaction at stripping section, and the isoprene that suppresses rectifying section takes place from dimerization reaction, this is that the present invention provides the basic reason of reflux ratio in 5～15 scopes, also be result through contriver's effort for many years, seem nuance, but effect significant difference, and the reflux ratio of this scope also can be implemented in industry, has industrial applicability.In addition, it is to be noted and in a rectifying tower, carry out reactive distillation processes, and all column plates that do not require this tower all are the column plates that helps reactive distillation, as long as adopt the column plate that helps reactive distillation just passable in spissated section of cyclopentadiene, the common column plate of employing can reduce other dimeric generation in other section.The column plate that helps reactive distillation is meant that the residence time, other column plate was longer relatively, for example increased overflow weir etc.The rectifying that will react in which column plate is determined in the distribution of body of the tower by each component.
The separating ring pentadiene method from cracked C 5 fraction of invention is compared with existing method, can not use the more hot dipolymer reactor of side reaction, compares with existing document and can really reduce secondary dimerization reaction, improves product quality.Be applied in the isoprene tripping device, can replace existing dipolymer reactor and pre-weight-removing column with a reaction fractionating tower.
Description of drawings
Fig. 1 is that expression utilizes reactive distillation separating ring pentadiene method of the present invention to produce the schema of m-pentadiene and dicyclopentadiene product.
Fig. 2 is the synoptic diagram that expression utilizes the one-section abstraction separating cracked carbon-5 fraction flow process of reactive distillation separating ring pentadiene method of the present invention.
Nomenclature:
1, reaction fractionating tower; 2, pre-lightness-removing column; 3, extraction tower; 4, Analytic Tower; 5, weight-removing column; 6, decarburization five towers; 7, m-pentadiene treating tower; 8, dicyclopentadiene treating tower.
Embodiment
Further explain the method and the application thereof of reactive distillation separating ring pentadiene of the present invention below in conjunction with accompanying drawing.
With reference to Fig. 1, cracked C 5 fraction is sent into reaction fractionating tower 1 middle part, comprise the logistics of isoprene from the cat head extraction through reactive distillation processes, comprise the logistics of m-pentadiene, cyclopentadiene and dicyclopentadiene from the extraction of tower still, described reactive distillation processes is meant that in rectifying initial ring pentadiene dimerization becomes the process of the reaction of dicyclopentadiene.
The logistics of reaction fractionating tower 1 tower still extraction is entered decarburization five towers 6, comprise the logistics of carbon five hydrocarbon from the 6 cat head extraction of decarburization five towers through rectifying or reactive distillation processes, enter dicyclopentadiene treating tower 8 from the logistics of decarburization five towers 6 tower still extraction, obtain the dicyclopentadiene product through rectifying.
The logistics that comprises carbon five hydrocarbon of decarburization five towers 6 cat head extraction enters m-pentadiene treating tower 7, through rectifying from m-pentadiene treating tower 7 tower stills or bottom side line extraction m-pentadiene product.
With reference to Fig. 2, further explain the application of method of the present invention in the one-section abstraction separating cracked carbon-5 fraction.
(1) the cracking c_5 raw material enters reaction fractionating tower 1 middle part, comprise isoprene and the more logistics of light constituent through reactive distillation processes from reaction fractionating tower 1 cat head extraction, enter pre-lightness-removing column 2 middle parts, comprise the logistics of carbon four and alkynes through rectifying in pre-lightness-removing column 2 cat head extraction, comprise the logistics of isoprene from the extraction of pre-lightness-removing column tower still;
(2) the described logistics that comprises isoprene enters extraction tower 3 middle parts, extraction solvent enters from extraction tower 3 tops, through the extracting rectifying process, the raffinate that comprises C 5 alkane and monoolefine from extraction tower 3 cat head extraction, enter Analytic Tower 4 from the logistics of tower still extraction, from the isoprene logistics of Analytic Tower 4 cat head extraction based on isoprene, the logistics of resolving the extraction of Tata still loops back extraction tower 3 through resolving;
(3) the isoprene logistics from Analytic Tower 4 cat head extraction enters weight-removing column 5 middle parts, through rectifying or reactive distillation processes from weight-removing column 5 cat head extraction isoprene products, from weight-removing column 5 tower still extraction heavy constituent.
Any solvent that described extraction solvent can be suitable for for example is dimethyl formamide, acetonitrile or N-Methyl pyrrolidone.
In the present invention, if do not particularly point out, degree is mass percentage content.
Cracked C 5 fraction with certain factory is a raw material, utilizes reactive distillation separation method of the present invention to carry out cracked C 5 fraction and separates, and raw material is formed and the turnover logistics of each operating gear is formed and is listed in the table below in 1.
(1) the cracking c_5 raw material is entered reaction fractionating tower 1 middle part, described reaction fractionating tower 1 is a plate distillation column, have 100 number of theoretical plates, the design residence time of every block of column plate is 15 seconds, reflux ratio is 8, tower top temperature is 45 ℃, comprise the logistics of isoprene from reaction fractionating tower 1 cat head extraction through reactive distillation processes, enter pre-lightness-removing column 2 middle parts, described pre-lightness-removing column 2 has 100 number of theoretical plates, and reflux ratio is 20, and tower top temperature is 40 ℃, comprise the logistics of carbon four and alkynes in pre-lightness-removing column 2 cat head extraction, comprise the logistics of isoprene from the extraction of pre-lightness-removing column tower still;
(2) the described logistics that comprises isoprene enters extraction tower 3 middle parts, extraction solvent enters from extraction tower 3 tops, extraction tower 3 has 90 theoretical stages, reflux ratio is 3, extraction solvent enters extraction tower 3 from top, solvent is a dimethyl formamide in the present embodiment, but the present invention is not limited to it, the charging mass flux ratio of solvent and carbon five hydrocarbon chargings is 5.5, through the extracting rectifying process, comprise the raffinate of C 5 alkane and monoolefine from extraction tower 3 cat head extraction, enter Analytic Tower 4 from the logistics of tower still extraction, Analytic Tower has 40 blocks of theoretical trays, reflux ratio is 1, tower top temperature is 50 ℃, and from the isoprene logistics of Analytic Tower 4 cat head extraction based on isoprene, the logistics of resolving the extraction of Tata still loops back extraction tower 3 through resolving;
(3) the isoprene logistics from Analytic Tower 4 cat head extraction enters weight-removing column 5 middle parts, weight-removing column has 160 number of theoretical plates, reflux ratio is 20, tower top temperature is 48 ℃, from weight-removing column 5 cat head extraction polymerization grade isoprene products, comprise the logistics of dicyclopentadiene through rectifying from weight-removing column 5 tower still extraction.
(4) logistics of the logistics of weight-removing column 5 tower still extraction and reaction fractionating tower 1 tower still extraction merges, enter decarburization five towers 6, decarburization five towers have 80 number of theoretical plates, reflux ratio is 15, tower top temperature is 45 ℃, comprise the logistics of carbon five hydrocarbon from the 6 cat head extraction of decarburization five towers through reactive distillation processes, enter dicyclopentadiene treating tower 8 from the logistics of decarburization five towers 6 tower still extraction, through rectifying from dicyclopentadiene treating tower 8 tower still side line extraction dicyclopentadiene products, the logistics that comprises carbon five hydrocarbon of decarburization five towers 6 cat head extraction enters m-pentadiene treating tower 7, through rectifying from m-pentadiene treating tower 7 tower still side line extraction m-pentadiene products.The plate number of m-pentadiene treating tower and dicyclopentadiene treating tower is identical with existing industrial installation with operating parameters.
As can be seen from Table 1, method of the present invention has improved the quality of m-pentadiene product and dicyclopentadiene product with respect to existing full scale plant, be applied in and utilize one-section abstraction just can obtain the polymerization grade isoprene product in the cracked C 5 fraction separating isoprene, separation process is shortened, simultaneously.In table 1, " other " mainly comprises components such as 2-methylpentane, benzene and toluene.Content is the barren place in the table 1, and routine analysis is adopted in expression, and analytical instrument does not detect this component or very micro-, the industrial content of generally ignoring them.
The turnover material of table 1 main device is formed (quality %)
The turnover material of table 1 (continuing) main device is formed (quality %)
Claims (5)
1. the method for cyclopentadiene in the reactive distillation separating cracked carbon-5 fraction, it is characterized in that, cracked C 5 fraction is sent into the reaction fractionating tower middle part, comprise the logistics of isoprene from the cat head extraction through reactive distillation processes, comprise the logistics of m-pentadiene, cyclopentadiene and dicyclopentadiene from the extraction of tower still, described reaction fractionating tower is a plate distillation column, have 70～160 number of theoretical plates, reflux ratio is 5～15, tower top temperature is 40～60 ℃, and described reactive distillation processes is meant that in rectifying initial ring pentadiene dimerization becomes the process of the reaction of dicyclopentadiene.
2. the method for claim 1 is characterized in that, the design residence time of every block of column plate on the top 1/3～1/2 of described reaction fractionating tower is 5～15 seconds, and the design residence time of every block of column plate of bottom 2/3～1/2 is 10～25 seconds.
3. method as claimed in claim 1 or 2, it is characterized in that, described method further comprises step: the logistics of reaction fractionating tower still extraction is entered decarburization five towers, comprise the logistics of carbon five hydrocarbon from decarburization five column overhead extraction through rectifying or reactive distillation processes, enter the dicyclopentadiene treating tower from the logistics of decarburization five Tata still extraction, obtain the dicyclopentadiene product through rectifying.
4. method as claimed in claim 3, it is characterized in that, described method further comprises step: the logistics that comprises carbon five hydrocarbon of decarburization five column overhead extraction enters the m-pentadiene treating tower, makes with extra care Tata still or bottom side line extraction m-pentadiene product through rectifying from m-pentadiene.
5. method as claimed in claim 3 is characterized in that, described decarburization five towers have 40～100 number of theoretical plates, and reflux ratio is 5～20, and tower top temperature is 40～60 ℃.
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| CN102040456A (en) * | 2009-10-20 | 2011-05-04 | 中国石油化工股份有限公司 | Method for preparing dicyclopentadiene and emulsifying packed tower used thereby |
| CN103992206B (en) * | 2014-06-05 | 2016-09-07 | 南京工业大学 | The method and system of prenol are prepared in a kind of ester exchange |
| CN105585415B (en) * | 2014-10-22 | 2017-11-07 | 中国石油化工股份有限公司 | A kind of method that reactive distillation prepares high purity dicyclo pentylene |
| CN105294382B (en) * | 2015-10-21 | 2018-01-02 | 河北工业大学 | A kind of method and its catalytic rectifying column of catalytic reaction rectification separating and cracking light dydrocarbon |
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| CN1253130A (en) * | 1998-11-09 | 2000-05-17 | 化学工业部北京化工研究院 | Method for separating diolefin from carbon five fraction |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
| CN101092319A (en) * | 2006-06-23 | 2007-12-26 | 天津天大天海化工新技术有限公司 | Method for separating cyclopentadiene |
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| CN1253130A (en) * | 1998-11-09 | 2000-05-17 | 化学工业部北京化工研究院 | Method for separating diolefin from carbon five fraction |
| CN1490286A (en) * | 2002-10-16 | 2004-04-21 | 中国石油化工股份有限公司 | Separating method for cracking C5-fraction |
| CN101092319A (en) * | 2006-06-23 | 2007-12-26 | 天津天大天海化工新技术有限公司 | Method for separating cyclopentadiene |
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