WO2022106685A1 - Destillationseinheit und verfahren zur trennung eines flüssigen stoffgemisches in 2 bis 6 flüssige produktströme unterschiedlicher zusammensetzung - Google Patents
Destillationseinheit und verfahren zur trennung eines flüssigen stoffgemisches in 2 bis 6 flüssige produktströme unterschiedlicher zusammensetzung Download PDFInfo
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- WO2022106685A1 WO2022106685A1 PCT/EP2021/082497 EP2021082497W WO2022106685A1 WO 2022106685 A1 WO2022106685 A1 WO 2022106685A1 EP 2021082497 W EP2021082497 W EP 2021082497W WO 2022106685 A1 WO2022106685 A1 WO 2022106685A1
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- Prior art keywords
- liquid
- evaporation
- devices
- distillation
- substances
- Prior art date
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- 238000004821 distillation Methods 0.000 title claims abstract description 125
- 239000000203 mixture Substances 0.000 title claims abstract description 97
- 239000007788 liquid Substances 0.000 title claims abstract description 91
- 239000000126 substance Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 43
- 239000012263 liquid product Substances 0.000 title claims abstract description 42
- 238000001704 evaporation Methods 0.000 claims abstract description 76
- 230000008020 evaporation Effects 0.000 claims abstract description 74
- 239000000047 product Substances 0.000 claims abstract description 55
- 230000008569 process Effects 0.000 claims abstract description 22
- CZZYITDELCSZES-UHFFFAOYSA-N diphenylmethane Chemical class C=1C=CC=CC=1CC1=CC=CC=C1 CZZYITDELCSZES-UHFFFAOYSA-N 0.000 claims description 58
- 229920001228 polyisocyanate Polymers 0.000 claims description 26
- 239000005056 polyisocyanate Substances 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 23
- 125000005442 diisocyanate group Chemical group 0.000 claims description 20
- 239000011552 falling film Substances 0.000 claims description 11
- 229920000768 polyamine Polymers 0.000 claims description 11
- 150000004985 diamines Chemical class 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 6
- 239000010409 thin film Substances 0.000 claims description 2
- 238000001944 continuous distillation Methods 0.000 abstract description 4
- 230000003134 recirculating effect Effects 0.000 abstract 1
- 238000009835 boiling Methods 0.000 description 11
- 239000007789 gas Substances 0.000 description 10
- 239000012071 phase Substances 0.000 description 8
- 238000004519 manufacturing process Methods 0.000 description 7
- 230000008901 benefit Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical class CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000012948 isocyanate Substances 0.000 description 3
- 150000002513 isocyanates Chemical class 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- IAQRGUVFOMOMEM-UHFFFAOYSA-N but-2-ene Chemical compound CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 229920000642 polymer Polymers 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000000998 batch distillation Methods 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000000539 dimer Substances 0.000 description 1
- XNMQEEKYCVKGBD-UHFFFAOYSA-N dimethylacetylene Natural products CC#CC XNMQEEKYCVKGBD-UHFFFAOYSA-N 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 229940127557 pharmaceutical product Drugs 0.000 description 1
- DGTNSSLYPYDJGL-UHFFFAOYSA-N phenyl isocyanate Chemical compound O=C=NC1=CC=CC=C1 DGTNSSLYPYDJGL-UHFFFAOYSA-N 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/06—Evaporators with vertical tubes
- B01D1/065—Evaporators with vertical tubes by film evaporating
-
- 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
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/82—Purification; Separation; Stabilisation; Use of additives
- C07C209/86—Separation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C263/00—Preparation of derivatives of isocyanic acid
- C07C263/18—Separation; Purification; Stabilisation; Use of additives
- C07C263/20—Separation; Purification
Definitions
- the present invention relates to a distillation unit (100000) designed for continuous distillation and a continuously operated process for separating a liquid mixture of substances (10) into 2 to 6 liquid product streams (201, 202, ...) of different composition and into a gaseous one product stream (300).
- an evaporation unit (10000) consisting of several evaporation devices (10000-1, 10000-2, ...) is provided, each evaporation device having a circulation device (1 200-1, 1 200-2, . . . ) for returning a portion of each of the liquid bottom streams (22, 21, . . . ) of an evaporation device to the respective evaporation device, each of these circulation devices also having a discharge device (1 300-1, 1 300-2, .. .) for providing one of the liquid product streams (201, 202, ).
- distillation systems are usually operated continuously, i.e. the mixture of substances to be distilled is fed continuously to the distillation column (in a defined volume flow) and the products of the distillation are continuously removed from the distillation column (again in defined Mcngcn.s/romcw ).
- continuous distillations are operated as long as the demand for the products requires it. This is to be distinguished from discontinuous distillation (also referred to as batch distillation), in which only a defined absolute amount of a mixture of substances to be separated is introduced into the distillation column and distilled.
- discontinuous distillations can only be operated until the submitted substance mixture is completely distilled. If further products of the distillation are then required, a new distillation process must be started.
- Discontinuous distillations are common for laboratory applications. In industrial processes, they are usually only used in the production of specialty chemicals or pharmaceutical products, where the quantities to be distilled are comparatively small.
- a discontinuous distillation of a multicomponent system using at least three distillation zones is described, for example, in US Pat. No. 6,550,274.
- the challenges in a batch operated distillation are significantly different from those of a continuously operated distillation (see US 6,550,274, column 4, lines 9 to 28).
- the present invention is only concerned with continuous distillation processes.
- a distillation column is fed continuously via an inlet with the mixture of substances to be separated, with a liquid phase consisting of comparatively high-boiling components being continuously discharged in the lower region of the distillation column (the so-called bottom of the column), while in the In the upper region of the distillation column (the so-called head of the column), a comparatively low-boiling distillate is continuously drawn off in liquid or gaseous form.
- a comparatively low-boiling distillate is continuously drawn off in liquid or gaseous form.
- the simultaneous continuous separation of a mixture of substances into two or more bottom products is particularly desirable when a plurality of bottom products can be obtained from the mixture of substances, but only one distillate. This is the case when the boiling point of the distillate phase is significantly lower than that of the bottom phase. In this case, different bottom products can be obtained by evaporating the distillation bottoms to different extents. Then the low-boiling distillate is recovered in (for example) two distillations of substantially the same composition but in different amounts, but with a different bottoms product being obtained in each of the distillations.
- DE 196 31 332 A1 deals with a method for removing disruptive high-boiling or solid components from the solvent cycle of regenerable absorption processes, such as e.g. B. gas scrubbing, liquid / liquid extractions or extractive distillations.
- Preferred embodiments include configurations of a regeneration column for regenerating a loaded solvent, in which the column has two continuously operated evaporators, one of which is used to adjust the concentration of a lower-boiling component in the solvent and the other is used to increase the concentration of the higher-boiling component Set component in the solvent.
- the unwanted high-boiling impurities are intermittently elutriated from the latter.
- the continuous production of two bottom products is not described.
- US 2008/016618 A1 deals with the separation of a mixture of «-butane, isobutane and various butene isomers.
- a distillation column is described which has a dividing wall running through the entire longitudinal section of the column body in its interior. Isobutene is obtained as a distillate. A stream of a mixture of 2-butene and n-butane and a stream of 1-butene are obtained in the two-part bottom of the column.
- the two bottom evaporators serve to heat a portion of each of the liquid bottom effluents from the column and recover it as liquid-vapor G'cm/.sc/? returned to the column.
- the bottoms evaporators are not designed to provide a liquid bottoms stream and a gaseous stream. Dividing wall columns have the fundamental disadvantage of being significantly more difficult to control than simple columns connected in series.
- WO 2017/005565 A1 deals with the problem of ensuring the uniform distribution of the liquid-vapor mixture formed in each stage to the next stage in distillations with multi-stage evaporation without having to accept other disadvantages such as stability problems in the design. The continuous production of two bottom products is not described.
- one subject of the present invention is a distillation unit (100000) for the continuous separation of a liquid mixture of substances (10) into n liquid product streams (201, 202, ... 20") of different composition and a gaseous product stream (300), wherein n is a natural number ranging from 2 to 6, where the distillation unit is (100000)
- distillation column (20000) for recovering the gaseous product stream (300), wherein the distillation column (20000) is not a dividing wall column, and
- (III) has at least one feed device (1 100-1, 1 100-2, ... 1 100- «) for introducing the liquid mixture of substances (10) to be evaporated, wherein the at least one feed device (1 100- 1, 1 100-2, ... 1 100- «)
- the evaporation unit (10000) has n evaporation devices (10000-1, 10000-2, ... 10000-'), from which the n liquid bottom streams (21, 22, ... 2ri) are taken, with im Case (IIIa) at least one of the n evaporation devices is assigned a feed device (1 100-1, 1 100-2, ... 1 100-") for introducing the liquid mixture of substances (10) to be evaporated, each of the n evaporation devices (10000-1, 10000-2, ... 10000-') via recirculation means (1 200-1, 1 200-2, ... 1 200-') for recycling a first portion of each of the removed ones n liquid bottom streams (21, 22, ...
- each of these n circulation devices (1 200-1, 1 200-2, ... 1 200-") also having a discharge Device (1 300-1, 1 300-2, ... 1 300-") for continuously providing one of the n liquid product streams (201, 202, ... 20"), each discharge device (1 300- 1, 1 300-2, ... 1 300- «) flow technically connected to the respective circulatory system (1 200-1, 1 200-2, ... 1 200- «).
- WO 2022/106685 'J'PCT/EP2021/082497 is that a second portion of each of the n liquid bottom streams (21, 22, ... In) via the discharge device (1 300-1, 1 300-2, ... 1 300- «) is discharged (ie this second portion can be identical to the corresponding liquid product stream (201, 202, ... 20«) or be a component thereof); and
- Another object of the present invention is a continuously operated process for separating a liquid mixture of substances (10) into n liquid product streams (201, 202, ... 20") of different composition and a gaseous product stream (300), where " is a natural number im range from 2 to 6, in which the separation is carried out in a distillation unit (100000) according to the invention.
- a “distillation unit (100000)” within the meaning of the invention consists of at least one “evaporation unit (10000)” which has “evaporation devices (10000-1, 10000-2, ... 10000-”), and a “distillation column (20000 )” as well as the peripheral devices required to carry out the separation of substances (pipes, pumps, condensers, heat exchangers and the like).
- the "n evaporation devices (10000-1, 10000-2, ... 10000-n)" are identical to “evaporators, as are known per se from the prior art, and the “evaporation unit (10000) “ is the total of all « evaporators (variant 1). However, it is also possible to divide one or more evaporators into a total of «chambers, which are then referred to as the “n evaporators (10000-1, 10000-2, ... 10000-n)” in the manner described in more detail below Sense of the invention are to be understood (variant 2). A combination of these two variants, i.e.
- distillation column (20000) Column-like devices known from the prior art for thermal material separation can be used as “distillation column (20000)” within the meaning of the invention.
- the desired target distillate is initially obtained in gaseous form as product stream (300) and can be continuously removed in gaseous form (300) from the distillation column via the discharge device (2300) and then condensed in a condenser. It is also possible to already integrate a condenser into the column body and to continuously remove the desired target distillate from the distillation column (20,000) already in liquid form as stream (310), as shown in the accompanying drawings.
- Feed, discharge and circulation devices as well as devices for receiving or returning streams of material produced during the distillation within the meaning of the invention are devices known to the person skilled in the art, such as in particular metal lines.
- the n evaporation devices (10000-1, 10000-2, ... 10000-") are arranged in one or more evaporators, each evaporator having 2 or more separate chambers for receiving the n liquid bottom streams (21, 22, ... 2n) and the total number of all chambers is n.
- case (IIIa) exists, wherein each of the n chambers has a feed device (1 100-1, 1 100-2, ... 1 100- «) for introducing the liquid mixture of substances (10) to be evaporated.
- the n evaporation devices (10000-1, 10000-2, . . . 10000-1) are n evaporators.
- case (IIIa) is present, in which each of the "evaporators" has a supply device (1 100-1, 1 100-2, ... 1 100 - «) for importing the liquid mixture of substances (10) to be evaporated.
- case (IIIa) is present, in which not each of the “evaporators” has a supply device (1 100-1, 1 100-2, ... 1 100- «) for importing the liquid mixture of substances (10) to be evaporated, wherein of each of the «evaporator, which has a feed device (1 100-1, 1 100-2, ... 1 100- «), a line leads from the respective circulation device (1 200-1, 1 200-2, ... 1 200- «) into the distillation column (20000).
- a first part of the "evaporation devices (10000-1, 10000-2, ... 10000-”) is in one or more evaporators each having 2 or more separate chambers for receiving liquid bottom streams ( 21, 22, 7) arranged, wherein a second part of the "evaporation devices (10000-1, 10000-2, ... 10000-”) consists of evaporators, where « is equal to 3 in particular.
- the chambers are one evaporators of different sizes.
- the evaporation unit (10000) comprises a thin-layer evaporator and/or a falling-film evaporator, with all evaporators used in particular being falling-film evaporators.
- case (IIIa) in which the liquid bottom stream from the distillation column (20000) is not fed into all of the "circulation WO 2022/106685 '°' PCT/EP2021/082497
- the liquid mixture of substances (10) comprises a mixture of di- and polyamines Diphenylmethane series, which are separated into n liquid product streams (201, 202, ... 20") comprising mixtures of di- and polyamines of the diphenylmethane series each with a different content of diamines of the diphenylmethane series and a gaseous product stream (300) comprising diamines of the diphenylmethane series.
- a first portion of the non-evaporated residual liquid (21) of the evaporator (10000-1) is returned to the top of the evaporator via the circulatory device (1200-1).
- a second portion of the non-evaporated residual liquid (21) is discharged via the discharge device (1300-1) and represents the first liquid product stream (201).
- the product (201) is therefore identical to the liquid bottom discharge ( 21) of the evaporator (10000-2). If, as shown in FIG.
- the liquid bottom product of the distillation column (20000) is fed via the device (line) 2200-1 into the circulation device (1200-2) of the evaporator (10000-2).
- the device (line) 2200-1 into the circulation device (1200-2) of the evaporator (10000-2).
- the liquid bottom product of the distillation column (20000) mixes with the liquid bottom product (22) of the evaporator (10000-2).
- a first portion of the mixture obtained in this way is fed to the top of the evaporator via the circulation device (1 300-2); a second subset is discharged via the discharge device (1300-2) as a second liquid product stream (202).
- each of the n evaporation devices (10000-1, 10000-2, ... 10000-n) has a circulation device (1 200-1, 1 200-2, ... 1 200 -n) for returning a first portion of each of the n liquid bottom streams (21, 22, ... 2n) removed to the respective evaporation device
- each of these n circulation devices (1 200-1, 1 200-2, ... 1 200-n) has a discharge device (1 300-1, 1 300-2, ... 1 300-n) for continuously providing one of the n liquid product streams (201, 202, ... 20n).
- the liquid mixture applied to the top of the evaporator (10000-2) via the circulation device (1200-2) runs through the evaporator from top to bottom and is partially evaporated.
- the gaseous stream (32) formed in this way which can also contain some of the entrained, non-evaporated liquid, is fed to the distillation column (20000) via the device (2100-2). There, the separation into the gaseous product stream (300) and the liquid distillation bottom stream takes place.
- the liquid bottom stream of the distillation column (20000) can also be fed to the circulation devices (1200-1, 1200-2) of both evaporators.
- These two embodiments are preferably combined.
- a feed pump for the bottom stream of the distillation column (20000) will generally be required.
- both are basically always possible: recycling of the bottom stream from the distillation column (20000) to a point in the circulation device (1 200-2) which, in terms of flow, is (i) behind or (ii) before the connection to the discharge device (1 300-2) to the circulatory device (1 200-2).
- Which of the two options is the better one depends on the boundary conditions and requirements of the individual case.
- an evaporation unit (10000) which has two evaporation devices (10000-1, 10000-2).
- the evaporation unit (10000) is an evaporator (a falling film evaporator shown here) which is divided into two chambers by installing a separating plate, each of which represents an inventive evaporation device (10000-1, 10000-2). Otherwise the reference numbers have the same meaning as before for FIG. 1 described.
- the feed stream of the mixture of substances (10) to be separated is divided between these two evaporation devices (10000-1, 10000-2).
- FIG. 1 is assigned its own circulation device (1 200-1 or 1 200-2), from which the respective liquid product stream (201 or 202) is removed.
- the baffle is shown in FIG. 2 shown offset by 90° for drawing reasons.
- FIG. 2b shows a cross-section directly below the heating tubes of the falling-film evaporator in a top view, showing the actual attachment of the device (2 100-1) to the evaporation unit (10000).
- the shown arrangement of the device (2 100-1) to the separating plate makes it possible for a gas phase (31) common to both evaporation devices (10000-1, 10 000-2) to be removed from the evaporation unit (10000) and fed to the distillation column (20000). becomes.
- the liquid bottom product of the distillation column (20000) is fed via the device (line) 2200-1 into the circulation device (1200-2) of the evaporation device (10000-1).
- FIG. 2a, b is one of several possibilities for designing variant 2 according to the invention.
- Other configurations are within the invention includes.
- it is possible to feed the material flow (10) to only one of the two evaporation devices (10000-1, 10000-2).
- This can also be implemented in a preferred manner by providing a feed device (1 100-1, 1 200-2) for each evaporation device (10000-1, 10000-2), but one of them is blocked by closing a valve (this is of course also possible when using evaporators that are not divided into chambers, as in variant 1 and variant 3).
- the evaporation unit (10000) includes a “conventional” evaporator (10000-1) and a second evaporator divided into two chambers (10000-1, 10000-2).
- the embodiment according to FIG. 3 has the advantage that the evaporator (10000-1) can be operated independently of the other evaporators. This enables high process stability in the event of strong concentrations and load changes.
- FIG. 3 is one of several possibilities for designing variant 3 according to the invention.
- the deviations discussed above for variants 1 and 2 of the specific embodiments shown in the illustrations can also be used in variant 3.
- At least one of the n circulation devices (1 200-1, 1 200-2, ... 1 200- ") with an adjustable (up to complete shut-off) supply line to one or more of the other n circulation facilities (1 200-1, 1 200-2, ... 1 200-n), with at least the circulation facilities (1 200-1, 1 200- 2, ... 1 200-"), which have such a supply line, are designed in such a way that the inflow from the relevant circulatory devices (1 200-1, 1 200-2, ... 1 200-") in the respective evaporation devices (10000-1, 10000-2, ... 10000- «) can be regulated (up to complete shut-off). This is shown in FIG.
- the discharge of the liquid product stream 202 via the device 1 300-2 is reduced in accordance with the reduced demand, with the quantity of liquid product stream 202 no longer being discharged via the device 1 300-2 being fed into the other evaporation device ( 10000-3).
- the evaporator output is reduced.
- the evaporation unit (10000) comprises a thin-film evaporator and/or a falling-film evaporator.
- all evaporators used are falling film evaporators. Falling film evaporators are characterized by a low thermal load and a short residence time on the heating surfaces. In principle, however, other types of evaporators are also conceivable. The only important thing is that the "liquid bottom streams (21, 22, . . . 2”)—possibly with the exception of the configuration with overflow lines (1 500-1, 1 500-2 . . . ) discussed above—are kept separate from one another .
- falling-film evaporators that are particularly preferred according to the invention can, with the exception of the subdivision of an evaporator into several vaporization chambers used in variant 2 and variant 3, be constructed in exactly the same way as is sufficiently known from the prior art.
- Falling film evaporators generally include at least the following technical devices, which are also preferably implemented in the present invention:
- the substance mixture to be separated is the at least one feed device (1 100-1, 1 100-2, ... 1 IOO-7) in the evaporation unit (10000) (case (IIIa), 'see above) or in the Distillation column (20000) (case (IIIb), 'see above) out.
- the liquid mixture of substances (10) to be separated is partially evaporated in the evaporation unit (10000), while the gaseous product stream (300) is obtained in the distillation column (20000).
- the "liquid product streams (201, 202, ... 20") are discharged via the discharge device (1 300-1, 1 300-2, ... 1 300-").
- the gaseous product stream (300) is removed from the distillation column (20000) either as such or in condensed form (310) via the discharge device (2300).
- Suitable temperatures and pressures for carrying out the process according to the invention can be easily determined by the person skilled in the art on the basis of his specialist knowledge, if necessary by carrying out simple preliminary tests, for any given separation task.
- the mixture of substances (10) to be separated is fed into the evaporation unit (10000), with the liquid bottom stream from the distillation column (20000) not being fed into all of the n circulation devices (1 200-1, 1 200 -2, ... 1 200-z?) (as also shown in FIG. 2a), in particular those of the n circuit devices (1 200-1, 1 200-2, ... 1 200-/ 7).
- the liquid product stream that has the lowest viscosity of all liquid product streams (201, 202, ... 20") (which is therefore the least concentrated) is provided, liquid bottom stream from the distillation column (20000) is supplied, wherein any existing devices (2200-1, 2200-2, .
- the gaseous product stream (300) separated off in this way comprises diisocyanates of the diphenylmethane series (as well as low-boiling secondary components and possibly minor proportions of (OCNjCeFLCFbCeFLfNCOjCFbCeFLlNCO) (so-called "3-nuclear MDI", which occurs in small proportions during the distillation in the distillation column (20000)"
- the distillate stream (310) can also contain traces of low-boiling impurities (such as phenyl isocyanate or solvent that has not been completely removed beforehand) and extremely small proportions (maximum 0.010% by mass, based on the total mass of the condensed distillate stream (310)) of entrained 3-core MDI.
- Condensation temperature (300-310): 80°C to 210°C, preferably 140°C to 170°C.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US18/253,606 US20240009591A1 (en) | 2020-11-23 | 2021-11-22 | Distillation unit and method for separating a liquid substance mixture into two to six liquid product flows with different compositions |
CN202180078364.XA CN116528956A (zh) | 2020-11-23 | 2021-11-22 | 用于将液体物质混合物分离成2至6个具有不同组成的液体产物料流的蒸馏单元和方法 |
EP21811374.4A EP4247508A1 (de) | 2020-11-23 | 2021-11-22 | Destillationseinheit und verfahren zur trennung eines flüssigen stoffgemisches in 2 bis 6 flüssige produktströme unterschiedlicher zusammensetzung |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP20209257.3 | 2020-11-23 | ||
EP20209257 | 2020-11-23 |
Publications (1)
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Citations (15)
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DE1208291B (de) * | 1957-12-31 | 1966-01-05 | Basf Ag | Kontinuierliches Verfahren zur destillativen Reinigung verdampfbarer organischer Stoffe von schwer oder nicht verdampfbaren Begleitstoffen |
US3309288A (en) * | 1962-11-02 | 1967-03-14 | Phillips Petroleum Co | Fractional distillation of a component from a feedstock by the addition of higher boiler vapors to the reboiler |
DE3106350A1 (de) * | 1980-03-25 | 1981-12-24 | Luwa AG, 8047 Zürich | Verfahren und einrichtung zur kontinuierlichen trennung fluessiger thermolabiler stoffgemische, insbesondere caprolactam, von verunreinigungen vorwiegend saurer natur oder von neutralen derivaten solcher verunreinigungen |
EP0141358A1 (de) * | 1983-10-28 | 1985-05-15 | Henkel Kommanditgesellschaft auf Aktien | Verfahren zur verbesserten destillativen Aufarbeitung von Glycerin |
DE19531806C1 (de) * | 1995-08-30 | 1997-04-10 | Henkel Kgaa | Verfahren zur schonenden Destillation von Fettsäuren |
DE19631332A1 (de) | 1996-05-21 | 1997-11-27 | Linde Ag | Entfernung störender Komponenten aus dem Lösemittelkreislauf von Gaswäschen |
EP0895982A1 (de) * | 1997-08-05 | 1999-02-10 | Basf Aktiengesellschaft | Verfahren zur Gewinnung von Hydroxypivalinsäureneopentyl-glykolester (HPN) |
JP2000302725A (ja) * | 1999-04-21 | 2000-10-31 | Daicel Chem Ind Ltd | 無水酢酸蒸留精製設備 |
US6498261B1 (en) * | 1995-06-07 | 2002-12-24 | Cognis Corporation | Process for improving color and color stability of oleic acid |
US6550274B1 (en) | 2001-12-05 | 2003-04-22 | Air Products And Chemicals, Inc. | Batch distillation |
US20080016618A1 (en) | 2006-07-21 | 2008-01-24 | O'shea Louise Ann | Patient Handling and Transfer Device |
WO2015197527A1 (de) | 2014-06-24 | 2015-12-30 | Covestro Deutschland Ag | Verfahren zur herstellung von di- und polyaminen der diphenylmethanreihe |
WO2017005565A1 (de) | 2015-07-03 | 2017-01-12 | Basf Se | Destillationseinrichtung umfassend eine kolonne, mit drei oder mehreren hintereinander flüssigkeitsdurchströmten zellen und verfahren zur destillation oder extraktivdestillation unter verwendung der destillationseinrichtung |
WO2017050776A1 (de) | 2015-09-24 | 2017-03-30 | Covestro Deutschland Ag | Verfahren zur herstellung von isocyanaten |
DE102018219557A1 (de) * | 2018-11-15 | 2020-05-20 | Thyssenkrupp Ag | Verfahren zur Herstellung und Reinigung von Propylenglykol |
-
2021
- 2021-11-22 EP EP21811374.4A patent/EP4247508A1/de active Pending
- 2021-11-22 US US18/253,606 patent/US20240009591A1/en active Pending
- 2021-11-22 CN CN202180078364.XA patent/CN116528956A/zh active Pending
- 2021-11-22 WO PCT/EP2021/082497 patent/WO2022106685A1/de active Application Filing
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DE1208291B (de) * | 1957-12-31 | 1966-01-05 | Basf Ag | Kontinuierliches Verfahren zur destillativen Reinigung verdampfbarer organischer Stoffe von schwer oder nicht verdampfbaren Begleitstoffen |
US3309288A (en) * | 1962-11-02 | 1967-03-14 | Phillips Petroleum Co | Fractional distillation of a component from a feedstock by the addition of higher boiler vapors to the reboiler |
DE3106350A1 (de) * | 1980-03-25 | 1981-12-24 | Luwa AG, 8047 Zürich | Verfahren und einrichtung zur kontinuierlichen trennung fluessiger thermolabiler stoffgemische, insbesondere caprolactam, von verunreinigungen vorwiegend saurer natur oder von neutralen derivaten solcher verunreinigungen |
EP0141358A1 (de) * | 1983-10-28 | 1985-05-15 | Henkel Kommanditgesellschaft auf Aktien | Verfahren zur verbesserten destillativen Aufarbeitung von Glycerin |
US6498261B1 (en) * | 1995-06-07 | 2002-12-24 | Cognis Corporation | Process for improving color and color stability of oleic acid |
DE19531806C1 (de) * | 1995-08-30 | 1997-04-10 | Henkel Kgaa | Verfahren zur schonenden Destillation von Fettsäuren |
DE19631332A1 (de) | 1996-05-21 | 1997-11-27 | Linde Ag | Entfernung störender Komponenten aus dem Lösemittelkreislauf von Gaswäschen |
EP0895982A1 (de) * | 1997-08-05 | 1999-02-10 | Basf Aktiengesellschaft | Verfahren zur Gewinnung von Hydroxypivalinsäureneopentyl-glykolester (HPN) |
JP2000302725A (ja) * | 1999-04-21 | 2000-10-31 | Daicel Chem Ind Ltd | 無水酢酸蒸留精製設備 |
US6550274B1 (en) | 2001-12-05 | 2003-04-22 | Air Products And Chemicals, Inc. | Batch distillation |
US20080016618A1 (en) | 2006-07-21 | 2008-01-24 | O'shea Louise Ann | Patient Handling and Transfer Device |
WO2015197527A1 (de) | 2014-06-24 | 2015-12-30 | Covestro Deutschland Ag | Verfahren zur herstellung von di- und polyaminen der diphenylmethanreihe |
WO2017005565A1 (de) | 2015-07-03 | 2017-01-12 | Basf Se | Destillationseinrichtung umfassend eine kolonne, mit drei oder mehreren hintereinander flüssigkeitsdurchströmten zellen und verfahren zur destillation oder extraktivdestillation unter verwendung der destillationseinrichtung |
WO2017050776A1 (de) | 2015-09-24 | 2017-03-30 | Covestro Deutschland Ag | Verfahren zur herstellung von isocyanaten |
DE102018219557A1 (de) * | 2018-11-15 | 2020-05-20 | Thyssenkrupp Ag | Verfahren zur Herstellung und Reinigung von Propylenglykol |
Also Published As
Publication number | Publication date |
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EP4247508A1 (de) | 2023-09-27 |
US20240009591A1 (en) | 2024-01-11 |
CN116528956A (zh) | 2023-08-01 |
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