Method of separating mixtures of isopentane-isoamylene-isoprene-containing hydrocarbon fractions or butane-butylene-divinyl hydrocarbon fractions

FIELD: chemistry.

SUBSTANCE: invention relates to a method of separating isopentane-isoamylene-isoprene-containing hydrocarbon fractions or butane-butylene-divinyl hydrocarbon fractions obtained at the first step of two-step dehydrogenation of corresponding paraffin hydrocarbons, involving separation of paraffin-olefin-diene fraction obtained at the first dehydrogenation step through extraction rectification, and is characterised by that a vapour stream is extracted from a desorber via lateral collection, where the said vapour stream contains large amount of diene, and after condensation, said stream is taken for extraction of the diene end product at the second extraction rectification step, and an olefin fraction which does not contain diene is collected from the top of the desorber and taken to the second dehydrogenation step.

EFFECT: use of said method increases output of the end product.

1 cl, 2 ex, 1 dwg

 

The invention relates to the field of separation of hydrocarbon mixtures containing unsaturated hydrocarbons, obtained in the first stage of two-stage dehydrogenation of the corresponding paraffin hydrocarbons by extractive distillation with a high-boiling polar extractants with subsequent desorption of unsaturated hydrocarbons from the extractant, in particular to the separation of isoprene from isopentane-isoamylene-sobrenatural faction and butadiene from butane-butylene-divinely fraction of the first stage dehydrogenation of isopentane and butane, respectively.

A known method of separation of dienes mixture of paraffins and olefins by a two-stage extractive distillation with a selective extractants, in which the fraction of C4or C5obtained in the first stage dehydrogenation using extractive distillation Argonauts paraffin, and the remaining olefin-diene fraction together with the olefin-diene fraction obtained in the second stage dehydrogenation of paraffin, is divided by means of extractive distillation for olefin and diene fraction (Ogorodnikov S. Kaliev, Idlis G.S. "the Production of isoprene." L.: Chemistry, 1973, pagination 126, 129).

The disadvantage of this method is the need for processing large quantities of olefin-diene fraction from the first stage dehydrogenation, the content of diene in which SOS is to place about 5%. Extractive distillation of this fraction on the column K-3 is associated with considerable difficulties, due to the high load of the column pairs of olefins, which leads to significant power consumption to maintain the required circulation of the extractant and create the desired reflux ratio.

The closest analogue to the technical nature of the invention is a method of separation of diene, wherein the olefin-diene fraction from the first stage dehydrogenation is sent to the second stage dehydrogenation without separating from it diene (Kirpichnikov P.A., Beresnev V.V., Popova L. "Album of technological schemes of the main industries of synthetic rubber" L.: Chemistry, 1986, p.16-17, 60-61).

The disadvantage of the closest analogue is the loss of a significant amount of the diene, as in the second stage dehydrogenation diene contained in the olefin fraction is converted into coke. It also adversely affects the catalyst of the second stage dehydrogenation, since the content of diene in the raw material fed to the dehydrogenation, should not exceed 1%.

The technical result is to increase the yield of the target product.

The technical result is achieved by the fact that in the proposed method of separating mixtures of hydrocarbons isopentane-isoamylene-sobrenatural faction or butane-butylene-divinely is racchi, obtained a two-step dehydrogenation of the corresponding paraffin hydrocarbons, which includes the separation obtained in the first stage dehydrogenation of paraffin-olefin-diene fraction using extractive distillation with desorber side selection output steam stream containing an increased amount of diene, and after condensation is directed to the selection of the target diene in the second stage extractive distillation, from the top of desorber selected olefinic fraction containing no diene, which is sent to the second stage dehydrogenation.

The essence of the technical solution is illustrated in the drawing, which shows a diagram of the installation for implementing the method.

Method of separating mixtures of hydrocarbons isopentane-isoamylene-sobrenatural faction or butane-butylene-divinely fraction is as follows.

Obtained in the first stage dehydrogenation of paraffin-olefin-diene fraction separated using extractive distillation. With desorber side selection output steam stream containing an increased amount of diene, and after condensation is directed to the selection of the target diene in the second stage extractive distillation. From the top of desorber selected olefinic fraction containing no diene, and sent to the second stage dehydrogenation. The operation is performed through a number of the LV 3, 11 and desorbers 5, 12 (see drawing).

The paraffin-olefin-diene fraction from the first stage dehydrogenation is supplied via line 1 in column 3 of extractive distillation. From the top of column 3 paraffin fraction is directed through line 2 to the first stage dehydrogenation. From columns 3 serves rich extractant in line 4 in desorber 5. In desorber 5 select steam stream containing an increased amount of diene, and after condensation is directed along the line 7 separation in column 11 of extractive distillation. From the top of desorber 5 selected olefinic fraction containing no diene that line 6 is directed to the second stage dehydrogenation. Desorbed extractant in line 15 is returned to the column 3.

In column 11 of extractive distillation serves on line 8 olefin-diene fraction from the second stage dehydrogenation. From the top of column 11 olefinic fraction along the line 10 is directed to the second stage dehydrogenation. From the column 11 serves rich extractant in line 14 in desorber 12. From the top of desorber 12 diene fraction in line 13 is supplied to the cleaning. Desorbed extractant in line 15 is returned to the column 10. To compensate for the loss of the extractant with a steam flow of desorber 5 part of the solvent after desorber 12 is directed in line 16 of circulating extractant first-stage extractive distillation (see drawing).

the example 1 comparative (nearest equivalent). In the process of emission of isoprene from the faction dehydrogenation of isopentane as the extractant used is anhydrous dimethylformamide (DMF). The quantity supplied to the separation of isopentane-isoamylene-isoprene fraction is 35 tons/hour. Fraction has the following composition, wt.%:

Paraffins (Σi-C5n-C5)60,88
Olefins (Σi-C5n-C5)36,66
Diene (Σi-C5n-C5)2,46

Circulation DMF is 140 tn/hour. For desorption of the absorbed hydrocarbons from saturated DMF use the column efficiency 57 plates. Rich extractant served on the 12-th plate (account below). Column operates at a pressure of top 1,04 ATA. The temperature of the top 35°C, the temperature of the cube 160°C.

Isopentane run, taken from the top of the extractive distillation column in the amount of 22 tons per hour, has the following composition, wt.%:

Waxes96,85
Olefins3,15

Isoamylene-isoprene fraction taken from the top of desorber in the amount of 13 tons per hour, the village is upusa to dehydration, has the following composition, wt.%:

Olefins93,37
Dieny6,63

When the separation of isopentane-isoamylene-isoprene fraction described by way of loss of diene are 0,86 t/h.

Example 2 (according to the claimed method). Desorption of hydrocarbons from saturated DMF carried out under conditions analogous to example 1. Side selection on the column 10 of the second stage of the extractive distillation is carried out from the 4th column plate 5 (desorber). The number of side selection is 7.5 tons/hour. Vaporous side selection has the following composition, wt.%:

Olefins0,6
Dieny11,4
DMF88

The distillate taken from the top of column 10 (desorber), in the amount of 13 tons per hour, entering the dehydrogenation, has the following composition, wt.%:

Olefins99,5
Dieny0,5

When the separation of isopentane-isoamylene-soprunova the fraction offered by way of loss of Dien amount of 0.07 tons/hour. The yield of the target product is increased.

Method of separating hydrocarbons isopentane-isoamylene-sobrenatural faction or butane-butylene-divinely fraction obtained in the first stage of two-stage dehydrogenation of the corresponding paraffin hydrocarbons, which includes the separation obtained in the first stage dehydrogenation of paraffin-olefin-diene fraction using extractive distillation, characterized in that desorber side selection output steam stream containing an increased amount of diene, and after condensation is directed to the selection of the target diene in the second stage extractive distillation, from the top of desorber selected olefinic fraction containing no diene, which is sent to the second stage dehydrogenation.



 

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< / BR>
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