WO2001054785A2 - Colonne compartimentee - Google Patents

Colonne compartimentee Download PDF

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Publication number
WO2001054785A2
WO2001054785A2 PCT/EP2001/000348 EP0100348W WO0154785A2 WO 2001054785 A2 WO2001054785 A2 WO 2001054785A2 EP 0100348 W EP0100348 W EP 0100348W WO 0154785 A2 WO0154785 A2 WO 0154785A2
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WO
WIPO (PCT)
Prior art keywords
column
chamber
section
boiler
mixture
Prior art date
Application number
PCT/EP2001/000348
Other languages
German (de)
English (en)
Other versions
WO2001054785A3 (fr
Inventor
Ulrich Kammel
Otto Machhammer
Peter Zehner
Original Assignee
Basf Aktiengesellschaft
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Basf Aktiengesellschaft filed Critical Basf Aktiengesellschaft
Priority to AU25158/01A priority Critical patent/AU2515801A/en
Publication of WO2001054785A2 publication Critical patent/WO2001054785A2/fr
Publication of WO2001054785A3 publication Critical patent/WO2001054785A3/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column

Definitions

  • the invention relates to a column for separating mixtures with at least three substances, with an outer shell which delimits an interior of the column and at least one column cover, and also with several partial chambers which extend over a section of the longitudinal extent of the column and are open on one side into the interior of the column, wherein a sub-chamber is designed as an inlet chamber, to which the mixture to be separated is fed, and at least one merging chamber, which adjoins the opening of at least two sub-chambers directed into the interior of the column.
  • a distillation column is proposed in EP 0 755 707 AI, the interior of which is divided into two partial chambers in the upper or lower part of the column with a vertical partition.
  • the partial chambers extend from the top or bottom of the column over a section of the longitudinal extent of the column and are open on one side into the interior of the column.
  • the subchambers each have their own condensers or evaporators.
  • the mixture of substances to be separated is fed in through a feed line which is arranged adjacent to the lower or upper end of the partition.
  • the separation of a te nary substance mixture using a distillation column according to EP 0 755 707 AI with two reinforcing columns and a stripping column is first described.
  • the component of the mixture of substances with the highest boiling point is referred to as high boiler, the component with the lowest boiling point as low boiler, and the component which has a boiling point between the boiling point of the high boiler and the low boiler, as medium boiler.
  • the ternary mixture is introduced into one of the subchambers, the feed being arranged near the lower end of the subchamber.
  • the higher-boiling fractions of the medium and high boilers are condensed out of the rising gas stream.
  • the condensate flows down and collects on a plate, which closes the feed chamber down to the stripping section of the column.
  • the condensate is discharged from the feed chamber through an opening provided at the lower end of the dividing wall into the stripping section of the column.
  • the condensate continues to flow downwards, whereby the low-boiling portions of the middle boiler are evaporated by rising hot gas flows.
  • a condensate rich in high boilers collects at the lower end of the column. It is discharged from the column and partially evaporated again using an evaporator.
  • the vaporized, gaseous phase is then reintroduced into the lower part of the column and rises to the top, where the higher-boiling fractions are condensed out by the condensate running downwards.
  • a gas connection between the stripping section of the column and the first rectifying section of the column, which is designed as an inlet chamber, is not provided.
  • the separation of the low boiler parts in the first compartment is therefore incomplete, which is why at the head of the second booster column removed medium boiler fraction is still contaminated with low boiler components.
  • the middle boiler fraction is still contaminated with parts of high boilers.
  • the ternary mixture of substances consisting of high boilers, medium boilers and low boilers, is introduced into the first stripping section designed as an inlet chamber.
  • the ternary mixture of substances is predominantly in the liquid phase.
  • the more volatile light and medium boilers are evaporated and escape through openings provided in a plate that closes off the feed chamber at the top into the upper rectifying section of the column.
  • the openings in the plate only allow gas to pass from the feed chamber into the upper rectifying section of the column, but do not allow liquid phase to pass from the rectifying section into the feed chamber. Portions of the high boiler transferred from the feed chamber into the rectifying section of the column are therefore condensed out with the middle boiler in the second partial chamber and contaminate the middle boiler fraction.
  • the object of the invention is to provide a column by means of which purer fractions of the middle boiler can be obtained.
  • a column for separating mixtures with at least three substances with an outer shell which delimits an interior of the column and at least one column cover, and also a plurality of subchambers which extend over a section of the longitudinal extent of the column and open on one side into the interior of the column , wherein a sub-chamber is designed as an inlet chamber to which the mixture to be separated is fed, and at least one union chamber which connects to the opening into the interior of the column of at least two sub-chambers, solved by the fact that the inlet of the mixture to be separated Mixing into the feed chamber occurs at a location spaced from the open end of the feed chamber in such a way that the inlet chamber is formed as a reinforcing column in the section adjoining the location of the supply line and in the section adjoining the location of the supply line as an output column.
  • the feed of the mixture to be separated into the feed chamber takes place at a distance from the open end of the feed chamber, in such a way that the feed chamber is designed as a reinforcing column in the section adjoining the location of the feed line on one side and in the other side the location of the feed line connecting section is designed as a stripping column, the individual fractions are better separated since the fraction separated in the feed part with the highest or with the lowest boiling point does not separate into the others because of the reinforcement or stripping section additionally provided in the feed chamber Chambers of the column is carried away.
  • the open end of the inlet chamber is understood to mean the end of the inlet chamber facing the interior, via which gas and liquid exchange takes place with the other chambers.
  • a unification chamber is understood to mean the section of the column which adjoins the subchambers in the interior of the column and extends over the opening of at least two subchambers directed into the interior of the column.
  • the section of the inlet chamber is understood to be the section which adjoins the inlet of the mixture to be separated into the inlet chamber in the direction of the rising hot gases.
  • An output section is understood to mean the section of the inlet chamber which, in the direction of the condensate flowing downward, adjoins the location of the feed of the mixture to be separated into the inlet chamber.
  • a deflection plate which is provided in the column according to EP 0 755 707, is provided in order to discharge the condensed phase in the case of the feed chamber being designed as a reinforcing column, or as a stripping part for removing the gaseous phase when the feed chamber is removed there is no provision for a mass transfer in the opposite direction in the column according to the invention.
  • an exchange connection between the inlet chamber and the union chamber is provided for the exchange of gaseous and liquid phases.
  • the plate can be designed, for example, as a bell bottom.
  • the exchange of liquid and gaseous phases is usually free under the influence of gravity or by convection.
  • the phases can also be exchanged by force. This is the case, for example, if different pressures are to prevail in the individual chambers because, for example, only one of the components of the mixture of substances is resilient up to a certain temperature.
  • a pump for the forced transport of the liquid phase is then provided in the exchange connection for the liquid phase.
  • a corresponding throttle element is provided in the exchange connection for the gaseous phase.
  • the partial chambers are arranged concentrically.
  • the feed chamber forms the outermost sub-chamber, which adjoins the inside of the shell of the column. Different temperatures or pressures can prevail in the subchambers. This causes the column material to expand to different extents.
  • the concentric arrangement of the partial chambers largely prevents warping or tensioning of the column.
  • the dividing wall is connected to the inner side of the shell of the column along at least one of its long sides.
  • the dividing wall then forms the individual subchambers with the shell of the column and possibly further dividing walls. It is common to all embodiments that there is no liquid exchange between subchambers arranged next to one another in the horizontal direction and that a mass exchange is effected only via the gas phase.
  • the partitions are usually flat. In order to counteract warping of the partition wall due to different temperature loads on the different sides, however, in one embodiment of the invention it is provided that the partition wall has a curvature.
  • a dividing wall can also be provided in the column, which is arranged at least in sections within a partial chamber.
  • partition walls are known for example from US 4,230,533.
  • the dividing walls generally designed as dividing plates, form chambers in the column which are open downwards and upwards in the longitudinal direction of the column.
  • Such dividing walls cause the, especially with large boiling point differences Components of a mixture of substances have a sufficient separating effect.
  • the person skilled in the art therefore has a means which, with sufficient boiling point differences, allows the mixture of substances to be separated easily.
  • the partitions can be constructed from segments. This enables the column to be easily matched to a particular separation problem by adapting the longitudinal extent of the chamber. Furthermore, the construction in segments offers the advantage that the partition walls have increased mobility, that is, lower stresses are built up due to temperature differences over the expansion of the partition wall.
  • the segments are advantageously held together by at least one tie rod.
  • the tie rod is arranged so that sufficient movement of the segments is guaranteed to counteract the build-up of stress.
  • the column is advantageously hung on its cover.
  • Fills, packs, internals or partitions can be provided in the subchambers or the unification chambers. It is also possible to install active packs that enable one or more substances to be converted during the distillation. Different beds, packs or internals in the subchambers can be combined as desired and the column can thus be tailored to a specific separation problem.
  • a great advantage of the column according to the invention is that different head pressures can be achieved in the individual subchambers. The head temperature in the individual subchambers can thus also be influenced. This enables a lowering of the temperature, for example when separating temperature-sensitive substances.
  • the column can also be designed such that the separation of mixtures with more than four components is possible is. For this purpose, several partition walls with different longitudinal dimensions are provided.
  • the partitions are designed in such a way that a section is formed between successive chambers, in which residues of the substance separated in the chamber previously arranged in the direction of increasing temperature are returned from the mixture of substances to be separated. In the direction of increasing boiling points of the separated components of the mixture of substances, the longitudinal expansion of partitions arranged next to one another increases.
  • Fig. 1 shows a longitudinal section through a column according to the invention
  • 3 a-1 is a schematic representation of different arrangements of the subchambers in cross section
  • Fig. 6 is a detailed view of the structure of a partial chamber
  • the column has a shell 1 which surrounds the interior of the column.
  • the interior is divided in the upper section of the column by a partition 2 into an inlet chamber 3 and a sub-chamber 4.
  • the partition 2 closes with the column Cover 5, so that a mass transfer between the feed chamber 3 and sub-chamber 4 is only possible via their open ends 6 and 7 directed towards the inside of the column.
  • the mixture of substances to be separated is introduced through the feed line 9 into the feed chamber 3 of the column.
  • the feed line 9 is arranged at a distance from the open end 6 of the feed chamber 3.
  • the portion of the high boiler fraction is fed back into the column through the steam feed 11.
  • the condensed liquid phase is at least partially returned to the feed chamber 3 via the feed line 13.
  • a steam discharge line 14 is provided, through which the vapor phase from the partial chamber 4 is fed to a condenser (not shown).
  • the condensed-out liquid phase can at least partly be fed back into the partial chamber 4 via the return line 15.
  • the column shown is designed in the unification chamber 8 as a bubble tray column.
  • the inlet chamber 3 and the sub-chamber 4 each have intermediate floors 16 which have openings 17 for gas and liquid exchange. Between the intermediate floors 16 and in section 3 a of the inlet chamber between the feed line 9 and the open end 6, internals, partitions, packs or beds 18 are provided. These can be different for the inlet chamber 3 and the sub-chamber 4.
  • the mixture to be separated is introduced as a vapor or liquid phase through feed line 9 into the feed chamber 3.
  • the gaseous fractions rise upward in the inlet chamber 3, the higher-boiling fractions being condensed out by the liquid phase flowing in counterflow from above.
  • the section 3a adjoining the inlet chamber 3 upwards acts as a reinforcing column.
  • the gaseous phase depleted in higher boiling fractions is nendeckel 5 out through the steam outlet 12 from the column. It is fed to a capacitor (not shown) in which condensation takes place at least in part.
  • the condensed-out liquid phase is at least partially fed back through the return line 13 to the upper region of the inlet chamber 3.
  • the liquid phase flows down through the inlet chamber 3, passing through the intermediate floors 16 through the openings 17.
  • the liquid phase depleted in lower-boiling fractions is passed out of the column via the bottom outlet 10 and at least partly fed to an evaporator (not shown). At least part of the liquid phase is at least partially evaporated and reintroduced into the combining chamber 8 of the column via the steam feed 11.
  • the recirculated portion of the at least partially vaporized liquid phase can either be only in vapor form or can also comprise two phases, ie liquid and vaporous portions.
  • the gaseous fractions rise, passing the bell bottoms through the chimneys 20.
  • the heavier boiling fractions are condensed out of the rising gases by the downward flowing liquid phase.
  • the hot gases pass into the inlet chamber 3 and the sub-chamber 4.
  • the gaseous fractions are at least partially condensed out there and at least some of the liquid phase is returned to the partial chamber 4 via the return line 15.
  • the liquid phase flows down through the sub-chamber A again, the more volatile components being evaporated again from the liquid phase by rising hot gases.
  • the head temperatures of the inlet chamber 3 and sub-chamber 4 are different.
  • the head temperature of the inlet chamber 3 is lower than the head temperature of the partial chamber 4.
  • the arrangement of the feed line 9, i.e. the distance to the open end 6 of the inlet chamber 3 is determined by the temperature difference between the boiling point, the low boiler fraction removed by steam discharge 12 and the medium boiler fraction removed by steam discharge 14. The smaller the temperature difference, the greater the distance between the feed line 9 and the open end 6 of the feed chamber 3, or the higher the separation performance of the internals.
  • FIG. 2a corresponds to the embodiment described in FIG. 1.
  • 2b corresponds to an embodiment for separating a mixture consisting of three fractions, the mixture consisting of a low boiler (A), a high boiler (C) and a medium boiler (B).
  • the boiling point of medium boiler B lies between the boiling points of low boiler A and high boiler C, its boiling point being closer to the boiling point of high boiler C.
  • the mixture of substances to be separated is fed to feed chamber 3 via feed line 9.
  • the liquid phase flows downwards, whereby the more volatile components are evaporated by rising hot gases.
  • the section 3b adjoining the feed line 9 in the feed chamber 3 acts as an output column.
  • the liquid phase which only contains high boilers, collects in the bottom of the feed chamber 3 and is discharged from the column through discharge line 21.
  • the liquid phase is at least partially fed to an evaporator 22 and at least partially evaporated again.
  • the vaporous or, if appropriate, also two-phase components are fed back into the feed chamber 3 via the steam return line 23, where the hot gases rise to the top. Due to the liquid components flowing downwards, the heavier-boiling components are again condensed out of the hot gas.
  • the rising hot gas passes through the location of the feed line 9.
  • portions of the high boiler fraction C which are still entrained in the gas mixture and which are entrained, for example, from the feed of the feed line 9 are carried away were condensed out by liquid components flowing down from the union chamber 8 from above.
  • the hot gas passes from the inlet chamber 3 into the confining chamber 8, the gaseous phase is therefore free from parts of the high boiler C.
  • the hot gas consisting of middle boilers B and low boilers A rises further upwards in the combination chamber 8, the liquid components flowing in opposite directions heavier boiling fractions of the medium boiler B are condensed out.
  • the hot gas of the low boiler A which is depleted in portions of the middle boiler B, is discharged through the steam outlet 24 and fed to a condenser 25.
  • the hot gas is at least partially condensed out and the condensate is returned to the union chamber 8 via return line 26.
  • a part of condensed low boiler fraction A can be removed via outlet 27.
  • the condensed liquid components flow downward in the combining chamber 8, with the more volatile components being evaporated again by the hot gas flowing upwards.
  • the liquid phase On its way down, the liquid phase enters both the inlet chamber 3 and the sub-chamber 4. Due to the liquid components entering the inlet chamber 3, higher-boiling components of the high boiler C are condensed out of the gas flowing upwards, at the same time more volatile components of the medium boiler B and the low boiler A are evaporated.
  • a pure liquid medium boiler fraction collects, which is led out of the sub-chamber 4 by a line 28.
  • Part of the discharged liquid phase of the middle boiler B is fed to the evaporator 29 and at least partially evaporated again. This portion is then fed again to the partial chamber 4 via the steam feed line 30.
  • Part of the pure medium boiler fraction B can be removed via outlet 31.
  • the hot gases returned to the sub-chamber 4 via the steam feed line 30 rise, the less volatile parts of the middle boiler B being condensed out again by liquid parts flowing from top to bottom.
  • the embodiments of the column shown in FIGS. 2a and 2b represent the two basic possibilities for arranging the dividing wall 2 in the upper section (FIG. 2a) of the column or in the lower section (FIG. 2b) of the column. Which of the two Embodiments is selected depends on the position of the boiling point of the medium boiler B relative to the boiling point of the high boiler C and the low boiler A. If the boiling point of the medium boiler B is closer to the boiling point of the low boiler A, the embodiment shown in FIG. 2a is suitable, in which the feed chamber 3 and the sub-chamber 4 are arranged in the upper section of the column. Is the boiling point of the middle boiler B closer to the boiling point of the high boiler C, the embodiment of the column shown in FIG. 2b is suitable.
  • FIGS. 2a and 2b For the separation of higher order mixtures, i.e. Mixtures of substances with several medium boiler fractions of different boiling points, the embodiments shown in FIGS. 2a and 2b can be combined as desired.
  • 2c shows an embodiment for a mixture with four substances, the substance mixture containing two low boilers (A, B) and two high boilers (D, C). Fraction A has the lowest boiling point, followed by fraction B, fraction C and finally fraction D, which has the highest boiling point.
  • the inlet 9 is arranged at a distance from the open end 6 of the inlet chamber 3 and that the partitions 2 and 2a overlap at least over part of their longitudinal extent.
  • the mixture of four components consisting of a low boiler A, a low-boiling medium boiler B, a low-boiling medium boiler C and a high boiler D is introduced via feed line 9 into the feed chamber 3.
  • the feed chamber 3 is separated into the low boiler A, which is drawn off at the top, and into a mixture of the higher-boiling components B, C and D.
  • the liquid which flows from top to bottom Part of components B, C, D runs down in the first union chamber, where the lower-boiling parts B and C are evaporated.
  • the portion of the substance mixture formed by the high boiler fraction D collects in the sump of the first union chamber 32.
  • the gaseous components D and C rise as hot gas into the inlet chamber 3, where they are condensed out again by the liquid portion flowing downward. Another portion of the gaseous components C and D enters the intermediate passage 33, in which gaseous portions of the high boiler D still present are condensed out by liquid portions passing from the top of the second union chamber 34 downward. A gas mixture therefore enters from the intermediate passage 33 the second union chamber 34, which contains no portions of the low boiler A and the high boiler D.
  • the hot gas mixture rises, the less volatile components being condensed out by liquid components flowing from top to bottom through the second combination chamber.
  • a pure middle boiler fraction B can therefore be taken off at the head of the second combination chamber. This is partially condensed and returned to the second union chamber.
  • the liquid phase flows downwards, whereby more volatile components are evaporated again by the rising gas stream.
  • the liquid fraction continues to decrease and on the one hand passes into the intermediate passage 33 and further into the first union chamber 32.
  • the more volatile components B and C are evaporated again and are conveyed back into the second combination chamber 34 with the gas stream.
  • Another portion of the liquid phase flowing downward from the second combination chamber 34 enters the sub-chamber 4, in which the more volatile components (B) are evaporated again by hot gas rising upward.
  • the fraction of the higher-boiling medium boiler C which can be removed from the column, collects in the bottom of sub-chamber 4. As in the embodiment shown in FIG. 2b, part of the fraction C is evaporated again and returned to the partial chamber 4 as a hot gas stream.
  • 2d shows an arrangement for a low boiler A, a middle boiler B with a somewhat higher boiling point, a middle boiler C with a boiling point slightly above the middle boiler B, and for a high boiler D.
  • the boiling points of components A, B and C are less than the distance from the boiling point of high boiler D.
  • the predominantly gaseous mixture of components A, B, C and D is introduced into feed chamber 3 via feed line 9.
  • the low boiler A is separated off.
  • the liquid components consisting of components B, C and D flow downward in the inlet chamber 3 and enter section 35 of the union chamber 8 about.
  • the section 35 extends from the lower end of the partition 2 to the lower end of the partition 2a.
  • the proportions of the medium boiler B are evaporated by rising hot gases.
  • the hot gases firstly pass into the inlet chamber 3, where they are condensed again, and into the partial chamber 4a, in which the hot gases of component B rise upwards and are withdrawn overhead.
  • Part of the gaseous component B discharged from the column is condensed out and returned to the sub-chamber 4a.
  • the liquid phase flowing downward condenses any remaining portions of the higher-boiling components D and C out of the rising gas stream.
  • the fraction of component B drawn off at the head of sub-chamber 4a is therefore free of impurities from components A, C and D.
  • the condensed out components D and C flow further down from section 35, the more volatile components of component C be vaporized by rising hot gas.
  • Pure high-boiling component D therefore accumulates at the bottom of the unification chamber 8 and can be passed out of the column at the bottom.
  • a portion of the high-boiling component D is at least partially evaporated again and returned to the column.
  • the parts of component C evaporated from the downward flowing liquid phase rise as hot gas, where they are either condensed again in section 35 or rise further in sub-chamber 4b and are taken off overhead as pure fraction C.
  • FIG. 2e shows an arrangement for a low boiler A, a high boiler D and two middle boilers B and C, the middle boiler C having a higher boiling point than the middle boiler B.
  • the boiling points of the middle boilers B and C are closer to the boiling point of the high boiler D as at the boiling point of the low boiler A.
  • the mixture of substances from the low boilers A, the medium boilers B and C and the high boilers D, which is predominantly in the liquid phase, is fed via a feed line
  • the inlet 9 fed to the inlet chamber 3.
  • the inlet 9 is spaced from the open end
  • the liquid mixture flows down, whereby as in the embodiment from FIG. 2b, components A, B and C are evaporated from the liquid phase by rising hot gases.
  • the liquid high boiler D collects, which, like in the other embodiments, is discharged from the inlet chamber 3 and is partly returned to the inlet chamber 3 as steam.
  • the vaporous mixture of components A, B and C rises as a hot gas stream and passes from the inlet chamber 3 into section 35. Due to the liquid phase running from top to bottom, the component with the highest boiling point, the middle boiler C, is condensed out of the vaporous mixture and collects in the bottom of the sub-chamber 4a.
  • the pure medium boiler C can be withdrawn from the column.
  • the gaseous components A and B rise from the section 35 of the combining chamber 8 to the top of the column, the component B being condensed out by the liquid phase flowing from top to bottom.
  • the middle boiler fraction B therefore accumulates in the sump of the sub-chamber 4b, from which pure middle boiler fraction B can be drawn off.
  • Pure low boiler fraction A is finally drawn off overhead. This is at least partially condensed and at least a portion of the condensed low boiler fraction A is returned to the union chamber 8.
  • the column according to the invention has been explained for a mixture of substances with three components (FIGS. 2a, b) and for a mixture of substances with four components (FIGS. 2c, d, e).
  • the column according to the invention can also be designed for mixtures with more than four components.
  • a correspondingly higher number of dividing walls will then have to be provided, the location of the arrangement, that is to say in the upper or in the lower part of the column, being determined by the distance between the boiling points of the components of the mixture. It is essential that at the open end of a single chamber there is an area for rectification, in which residues of the component are still separated from the mixture and are separated in this chamber before the mixture passes into the next chamber.
  • this area corresponds to the rectification with respect to the sub-chamber 4a Section 35, by still separating residues of medium boilers B from the mixture.
  • the section between the inlet and the open end of the inlet chamber also has the same effect in the case that, in the case of the arrangement from FIG. 2a, remnants of the low boiler A or in the case of the arrangement from FIG become.
  • the subchambers do not always have to extend from the top or bottom of the column.
  • 2f shows an inlet chamber 3, the closed end 36 of which is spaced in the longitudinal direction from the column head or column cover 5.
  • a dividing wall is understood to mean a dividing plate arranged in the longitudinal direction in the column, which in the column produces a compartment which is open in the direction of the column head and of the column bottom. Embodiments with a dividing plate are shown in the figures in FIGS. 2g to i.
  • a mixture consisting of four components is introduced into the feed chamber 3 via the feed line 9.
  • the low boiler A which is removed overhead from the feed chamber 3
  • the higher-boiling components B, C and D which flow downward from the feed chamber 3 in condensed form. They enter a first section 38 which extends in the longitudinal direction from the lower end of the dividing wall 2 to the lower end of the dividing wall 37 and is delimited on its sides by the casing 1 and the dividing wall 37.
  • the predominant portion of component B and a certain portion of component C are evaporated by rising hot gases, component C having a higher boiling point than component B.
  • the liquid phase depleted in components B and C occurs in a second Section 39, which connects to the first section 38 in the longitudinal direction below the lower end of the partition wall 37. Downward is the second section 39 closed off from the column sump. As it continues to sink, the volatile constituents are evaporated from the liquid phase, so that a pure high boiler fraction D collects at the bottom, which can be removed from the column.
  • the gaseous components, predominantly medium boilers C and residues of the high boiler D rise to the top.
  • the hot gases either re-enter the first section 38, where the gaseous components of component C are partially condensed out again, or the more volatile components are combined with the more volatile gaseous components coming from the inlet chamber 3 through the third section 40 is delimited to the sides by the dividing wall 2 and the dividing wall 37 and is open upwards and downwards, upwards into the fourth section 41.
  • the fourth section 41 extends from the upper end of the dividing wall 37 to the top of the column and becomes the Sided by the partition 2 and the shell 1. In section 41, the less volatile components of the liquid phase flowing downward are condensed out, so that a pure middle boiler fraction B can be removed at the top of the fourth section 41.
  • the fifth section 42 which is to the sides of the dividing wall 37 and Envelope 1 is limited and is open at the top and bottom.
  • a hot gas phase occurs from below, which mainly consists of component C. It rises in the fifth section 42 and can via the exit
  • the mixture is not fed directly into the feed chamber.
  • the low-boiling components A are initially separated off, while the higher-boiling components B to D or B to E flow downward.
  • the lower end of the chamber formed by the partition wall 37 is to be regarded as the inlet chamber in these embodiments.
  • the location according to the invention of the feed into the inlet chamber is identified in FIGS. 2h and i by reference numerals 9 '. In these embodiments, too, a reinforcing part and an output column are formed in the inlet chamber.
  • packings or fillings can be provided in the subchambers or the unification chambers. Examples of such embodiments are shown schematically in FIGS. 2j and k. In terms of their basic structure, these two embodiments correspond to the embodiment shown in FIGS. 2a and 1.
  • the inlet chamber 3 and the union chamber 8 contain packs, while the sub-chamber contains 4 internals. In the exemplary embodiment shown, these are dividing floors.
  • the inlet chamber 3 contains a bed, for example glass rings, while the sub-chamber contains 4 packs. Internals are provided in the union chamber. Basically all packings, beds or internals available on the market can be used for the column according to the invention. Active packs can also be used, which enable one or more components to be converted during the distillation. The person skilled in the art selects the appropriate packs, beds or internals for a given separation problem.
  • 21 shows a special embodiment of the column shown in FIGS. 1 and 2a.
  • the inlet chamber 3 and the sub-chamber 4 are not separated by a partition, but are designed as independent column branches, the outer wall of which is formed in front of the casing 1. The mixture of substances is separated in the same way as described in FIG. 1.
  • 2m shows an embodiment in which the pressure in the feed chamber is lower than in the union chamber 8 or the subchamber 4.
  • the mixture of substances to be separated is introduced into the feed chamber 3 via the feed line 9.
  • the mixture of substances is formed by a low boiler A, a medium boiler B and a high boiler C. There, the low boiler is evaporated by rising hot gases and is finally led out of the column through steam outlet 12.
  • the discharged steam is condensed and at least partially returned to the inlet chamber 3 via the return line 13. There the condensate flows downwards, whereby volatile constituents are evaporated and less volatile constituents are condensed out of the gas phase.
  • Condensate which consists of the middle boiler B and the high boiler C, collects on the bottom 101. The condensate is discharged via line 102 with the aid of the pump 103 and is forcibly fed to the union chamber 8.
  • the throttle body 104 By the throttle body 104, the rising gas from the higher pressure in the union chamber 8 to the lower pressure of Inlet chamber 3 relaxed.
  • FIG. 3 shows a cross section through the column according to the invention, the position of the section being laid through the section of the column in which the subchambers or feed chamber are arranged.
  • 3a to f show exemplary arrangements for a mixture of three components, while the arrangements shown in FIGS. 3 g to 1 show examples of a mixture with four components.
  • the casing is designated by the reference number 1 and the partition by the reference number 2 or 2a and 2b.
  • 3 a shows a division in which the cross section through the partition 2 is divided into two even halves. Depending on the proportions of the components contained in the mixture to be separated, however, other ratios can also be selected.
  • 3b shows an arrangement of the partition 2, the cross section being divided in a ratio of 2: 1 or in FIG. 3c in a ratio of 3: 1.
  • 3b and c the partition 2 is formed in each case by two sheets arranged at an angle to one another.
  • FIG. 3d shows an embodiment with a curved partition 2. With the embodiment shown in FIG. 3d, expansion phenomena due to temperature fluctuations can be mastered more easily.
  • the embodiments shown in FIGS. 3e and f are particularly advantageous. 3e, the partial chambers are arranged concentrically.
  • one of the subchambers is divided into several tubes.
  • the phase contained in the tubes is united in the upper or lower part by a common space that is connected to all tubes.
  • FIGS. 3 g to 1 an arrangement with two parallel planar partitions 2a and 2b is shown.
  • 3h shows an arrangement with three circular segments, each of which forms a partial chamber and is separated by a partition 2.
  • 3j shows a concentric arrangement of three subchambers.
  • Fig. 3k an arrangement with two tubes, each tube being used to separate a certain component different from the component separated in the other tube. Any combination is conceivable.
  • Combinations of annular and planar partitions are shown by way of example in FIGS. 3i and 1.
  • FIG. 4 and 5 show the two possibilities for the arrangement for separating a mixture of three components in greater detail.
  • 4 corresponds to the embodiment shown in FIG. 1 or FIG. 2a and FIG. 5 corresponds to the embodiment shown in FIG. 2b.
  • FIG. 4 To separate the individual components, please refer to the relevant sections.
  • FIG. 4 several intermediate floors 16 are arranged in the inlet chamber 3. Packing material can be arranged on these shelves, for example.
  • the gaseous components are discharged through steam discharge 12 from the inlet chamber or steam discharge 14 from the partial chamber 4.
  • the column has a column cover 5 on which the column is suspended. At the lower end, the column is freely stored. In this way, tensions caused by temperature fluctuations within the column and the associated different material expansion can be compensated.
  • FIG. 5 shows the embodiment corresponding to FIG. 2b in more detail.
  • the feed chamber 3 also contains intermediate floors 16.
  • the intermediate floors are also provided in the union chamber 8.
  • the column in turn has a column cover 5 on which the column is suspended.
  • Fig. 6 shows in greater detail the structure of the intermediate floors 16, as used for example in the inlet chambers 3 in the embodiments of Figs. 4 and 5.
  • Two intermediate floors 16 lying one above the other are each braced against one another along one of their sides by a tie rod 43 and thus fixed.
  • a shirt 44 is fastened to the underside of the intermediate floor 16 on the opposite side. This engages with its lower end in a seal 45 arranged on the outer edge of the intermediate floor 16 arranged underneath.
  • the seal 45 consists of a U-shaped profile which encloses the edge of the shirt on one side. Liquid is contained, for example, between the shirt and the U-shaped profile, which ensures that the space between two intermediate floors 16 is sealed off from the outside.
  • the structure chosen can be used to compensate for stresses which occur due to temperature differences over the length of the column.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Extraction Or Liquid Replacement (AREA)

Abstract

L'invention concerne une colonne destinée à la séparation de mélanges constitués d'au moins trois matières, comprenant : une enveloppe extérieure (1) délimitant un volume intérieur de la colonne ; au moins un couvercle de colonne (5) ; plusieurs sections (3, 4) ouvertes sur un seul côté à l'intérieur de la colonne et s'étendant sur une partie de la longueur de la colonne. Une de ces sections constitue une chambre d'alimentation (3), vers laquelle est dirigée le mélange à séparer. Ladite invention comprend également au moins une section de réunion (8), raccordée à l'ouverture orientée à l'intérieur de la colonne d'au moins deux sections (3, 4). L'invention est caractérisée en ce que l'alimentation du mélange à séparer dans la chambre d'alimentation (3) s'effectue en un point espacé de l'extrémité ouverte de la chambre d'alimentation (3), de telle manière que cette dernière est façonnée comme une colonne de concentration (3a) dans la partie adjacente à l'un des côtés du point d'alimentation, et comme une colonne de rectification dans la partie (3b) adjacente à l'autre côté du point d'alimentation. Des mélanges complexes peuvent ainsi être séparés en fractions plus pures, les dépenses en matière d'appareillage et d'énergie étant moindres par rapport à celles de colonnes montées en série.
PCT/EP2001/000348 2000-01-24 2001-01-12 Colonne compartimentee WO2001054785A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU25158/01A AU2515801A (en) 2000-01-24 2001-01-12 Column with multiple shafts

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10002806.3 2000-01-24
DE2000102806 DE10002806A1 (de) 2000-01-24 2000-01-24 Multishaft-Kolonne

Publications (2)

Publication Number Publication Date
WO2001054785A2 true WO2001054785A2 (fr) 2001-08-02
WO2001054785A3 WO2001054785A3 (fr) 2001-12-27

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AU (1) AU2515801A (fr)
DE (1) DE10002806A1 (fr)
TW (1) TW496750B (fr)
WO (1) WO2001054785A2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2016530086A (ja) * 2013-07-18 2016-09-29 エルジー・ケム・リミテッド 分離壁型蒸留塔

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10258160A1 (de) * 2002-12-12 2004-06-24 Basf Ag Verfahren und Vorrichtung zur Extraktivdestillation
DE102004022735A1 (de) * 2004-05-07 2005-12-01 Vinnolit Gmbh & Co. Kg Geteilte EDC-Kolonne
DE102004024688A1 (de) * 2004-05-19 2005-12-15 Basf Ag Trennwandkolonne
DE102004052593B4 (de) * 2004-10-29 2020-03-26 Rehm Thermal Systems Gmbh Vorrichtung und Verfahren zur Aufbereitung eines Wärmeübertragungsmediums für eine Kondensationsaufschmelzlötanlage
GB0920541D0 (en) * 2009-11-24 2010-01-06 Doosan Babcock Energy Ltd Column
DE102013226428A1 (de) * 2013-12-18 2015-06-18 Basf Se Extraktionskolonne und Verfahren zum Extrahieren eines Bestandteils aus einem Fluid

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1194599A (en) * 1967-02-23 1970-06-10 Universal Oil Prod Co Distillation method and apparatus
US4419188A (en) * 1980-06-02 1983-12-06 Mccall Thomas F Thermally coupled extractive distillation process
EP0133510A1 (fr) * 1983-08-03 1985-02-27 BASF Aktiengesellschaft Procédé de séparation par distillation d'un mélange azéotropique
EP0638778A1 (fr) * 1993-08-05 1995-02-15 Praxair Technology, Inc. Système de destillation avec colonne compartimentée
DE19806324C1 (de) * 1998-02-05 1999-06-24 Mannesmann Ag Verfahren und Anlage zur Fraktionierung von Gaskondensaten oder leichtem Rohöl
US6077985A (en) * 1999-03-10 2000-06-20 Kellogg Brown & Root, Inc. Integrated deethanizer/ethylene fractionation column

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1194599A (en) * 1967-02-23 1970-06-10 Universal Oil Prod Co Distillation method and apparatus
US4419188A (en) * 1980-06-02 1983-12-06 Mccall Thomas F Thermally coupled extractive distillation process
EP0133510A1 (fr) * 1983-08-03 1985-02-27 BASF Aktiengesellschaft Procédé de séparation par distillation d'un mélange azéotropique
EP0638778A1 (fr) * 1993-08-05 1995-02-15 Praxair Technology, Inc. Système de destillation avec colonne compartimentée
DE19806324C1 (de) * 1998-02-05 1999-06-24 Mannesmann Ag Verfahren und Anlage zur Fraktionierung von Gaskondensaten oder leichtem Rohöl
US6077985A (en) * 1999-03-10 2000-06-20 Kellogg Brown & Root, Inc. Integrated deethanizer/ethylene fractionation column

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2016530086A (ja) * 2013-07-18 2016-09-29 エルジー・ケム・リミテッド 分離壁型蒸留塔
US10384146B2 (en) 2013-07-18 2019-08-20 Lg Chem, Ltd. Divided wall distillation column

Also Published As

Publication number Publication date
DE10002806A1 (de) 2001-07-26
AU2515801A (en) 2001-08-07
TW496750B (en) 2002-08-01
WO2001054785A3 (fr) 2001-12-27

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