WO2000058255A1 - Verfahren zur destillativen auftrennung eines flüssigen rohaldehydgemisches - Google Patents
Verfahren zur destillativen auftrennung eines flüssigen rohaldehydgemisches Download PDFInfo
- Publication number
- WO2000058255A1 WO2000058255A1 PCT/EP2000/002721 EP0002721W WO0058255A1 WO 2000058255 A1 WO2000058255 A1 WO 2000058255A1 EP 0002721 W EP0002721 W EP 0002721W WO 0058255 A1 WO0058255 A1 WO 0058255A1
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- WIPO (PCT)
- Prior art keywords
- aldehyde
- product stream
- straight
- chain
- distillation column
- Prior art date
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- 238000004821 distillation Methods 0.000 title claims abstract description 51
- 239000000203 mixture Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 26
- 125000002485 formyl group Chemical class [H]C(*)=O 0.000 title claims abstract 26
- 239000007788 liquid Substances 0.000 title abstract description 11
- 238000009835 boiling Methods 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims description 23
- 238000012856 packing Methods 0.000 claims description 8
- 238000007700 distillative separation Methods 0.000 claims description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims 2
- 150000001299 aldehydes Chemical class 0.000 description 90
- 239000000047 product Substances 0.000 description 34
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 24
- AMIMRNSIRUDHCM-UHFFFAOYSA-N Isopropylaldehyde Chemical compound CC(C)C=O AMIMRNSIRUDHCM-UHFFFAOYSA-N 0.000 description 24
- 239000000470 constituent Substances 0.000 description 13
- 238000007037 hydroformylation reaction Methods 0.000 description 12
- YGHRJJRRZDOVPD-UHFFFAOYSA-N 3-methylbutanal Chemical compound CC(C)CC=O YGHRJJRRZDOVPD-UHFFFAOYSA-N 0.000 description 10
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N pentanal Chemical compound CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 10
- 238000010992 reflux Methods 0.000 description 8
- 150000001298 alcohols Chemical class 0.000 description 4
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- IAQRGUVFOMOMEM-UHFFFAOYSA-N but-2-ene Chemical compound CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- FJJYHTVHBVXEEQ-UHFFFAOYSA-N 2,2-dimethylpropanal Chemical compound CC(C)(C)C=O FJJYHTVHBVXEEQ-UHFFFAOYSA-N 0.000 description 2
- BYGQBDHUGHBGMD-UHFFFAOYSA-N 2-methylbutanal Chemical compound CCC(C)C=O BYGQBDHUGHBGMD-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000005094 computer simulation Methods 0.000 description 2
- 239000007859 condensation product Substances 0.000 description 2
- 239000000539 dimer Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 239000013638 trimer Substances 0.000 description 2
- 239000001893 (2R)-2-methylbutanal Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- XNMQEEKYCVKGBD-UHFFFAOYSA-N dimethylacetylene Natural products CC#CC XNMQEEKYCVKGBD-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- -1 n-valeraldehyde Chemical compound 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 238000010561 standard procedure Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
- C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/78—Separation; Purification; Stabilisation; Use of additives
- C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S203/00—Distillation: processes, separatory
- Y10S203/20—Power plant
Definitions
- the present invention relates to a process for the distillative separation of a liquid crude aldehyde mixture which essentially comprises 95 to 99.9% by weight, based on the total weight of the product mixture, of a straight-chain and a branched aldehyde.
- Aldehydes are produced on an industrial scale by hydroformylation of olefins in the presence of cobalt or rhodium catalysts. While it is generally desirable to obtain straight chain aldehydes; depending on the hydroformylation conditions, mixtures of straight-chain and branched aldehydes are obtained. In addition to the aldehydes, high-boiling aldehyde condensation products, such as dimers, trimers and tetramers of the aldehydes, and by reducing the aldehydes, the corresponding alcohols are formed as by-products in the hydroformylation.
- the reaction mixture obtained in the hydroformylation must therefore be separated. This is usually done by a two-stage distillation process using two separate, approximately equally dimensioned distillation columns. The entire aldehyde is separated from the high-boiling constituents in the first column. The mixture of straight-chain and branched aldehyde is then separated in the second column.
- the process consists of using only one distillation column for the separation of the crude aldehyde mixture and selecting the distillation conditions so that the branched aldehydes are removed in liquid form in the upper region of the distillation column and the straight-chain aldehyde is broken down into two product streams.
- the first product stream which is essentially pure, straight-chain aldehyde, is taken off in vapor form in the lower region of the distillation column.
- the amount of this aldehyde product Current is not more than 70% by weight of the total amount of straight-chain aldehyde in the crude aldehyde mixture.
- the second product stream of straight-chain aldehyde is taken off at the bottom, it contains the majority of the high-boiling components.
- the process does indeed allow the branched aldehydes, the straight-chain aldehydes, to be separated off. but are only separated into two fractions of different purity, the amount of the first relatively pure fraction max. It is 70% of the product used in order not to allow the amount of high-boiling components in the second fraction to rise too high.
- the amount of pure straight-chain aldehyde that can be achieved in practice with this method is thus only max. 70% by weight of the straight-chain aldehyde present in the crude product mixture.
- the present invention is therefore based on the object of providing a process for the separation of a liquid crude aldehyde mixture which is less complex and allows the straight-chain and the branched aldehyde to be obtained as completely as possible in pure form.
- the present invention therefore relates to a process for the distillative separation of a crude aldehyde mixture which comprises essentially 94 to 99.8% by weight, based on the total weight of the crude aldehyde mixture, of a straight-chain and one or more branched aldehydes (straight-chain and branched alcohols have the same Contains carbon number), the method being characterized in that
- A) the crude aldehyde mixture is fed into the middle region of a first distillation column with several separation stages and carries out a separation therein
- a first aldehyde product stream which is taken off above or close to the top of the distillation column and essentially comprises pure branched aldehyde
- a second aldehyde product stream taken off directly above or above the evaporator in the region of the first 20% of the total separation stages and comprising substantially pure straight chain aldehyde
- the further product stream at the bottom of the first distillation column decreases and passes into a second distillation column, the packing volume of which is 50 to 200 times smaller than that of the first distillation column, and therein into a product stream which comprises essentially pure straight-chain aldehyde and is taken off overhead or close to the top of the second distillation column, and is separated into a product stream which essentially comprises the high-boiling constituents.
- FIG. 1 shows a schematic representation of the method according to the invention.
- Hydroformylation is a known process which is described, for example, in US Pat. Nos. 4,148,830; 4,247,486; 4,593,127 and in EP 404 193 and EP 484 977 A.
- olefins with three or four carbon atoms such as propylene, 1-butene, 2-butene (ice or trans) and isobutylene, are used as the starting material for the hydroformylation.
- the crude aldehyde mixture to be separated according to the invention therefore preferably contains straight-chain and branched C- or Cs-aldehydes.
- the catalysts used for the hydroformylation are also known; they are described, for example, in the patent publications cited in EP 484 977 A.
- the crude aldehyde mixture obtained in the hydroformylation contains, in addition to lower-boiling constituents, such as carbon monoxide and hydrogen, branched aldehydes, straight-chain aldehydes and higher-boiling constituents.
- lower-boiling constituents such as carbon monoxide and hydrogen
- branched aldehydes straight-chain aldehydes and higher-boiling constituents.
- the latter are by-products which are formed by condensation of the aldehydes to give dimers, trimers and tetramers and by reduction of the resulting aldehydes with hydrogen to the corresponding alcohols.
- the crude aldehyde mixture in particular the hydroformyl tion of C-aldehydes obtained from propylene, such as n-butyraldehyde and isobutyraldehyde, or the C 5 -aldehydes obtained by hydroformylation of butene, such as n-valeraldehyde, and the branched Cs-aldehydes, 2-methylbutyraldehyde, 3-methylbutyraldehyde and pivalaldehyde , contain.
- the composition of the crude aldehyde mixtures depends on the conditions of the hydroformylation process.
- the weight ratio of straight chain aldehyde to branched aldehyde (s) is generally in the range of about 8: 2 to about 99: 1.
- the total amount of aldehydes in the crude aldehyde mixture is generally 94 to 99.8% by weight, preferably 97 to
- the rest is formed by the above-mentioned lighter and in particular the higher-boiling constituents, namely in each case approximately 0.1 to 3% by weight of the condensation products and the alcohols.
- the process according to the invention can be carried out in any suitable distillation column.
- tray columns such as valve tray columns, and preferably columns with packings are suitable.
- the packs can be customary random packs or ordered packs, the latter being preferred.
- the package used is Mellapak® from Sulzer (ordered package).
- the number of theoretical plates must be large enough to achieve the desired separation. It is generally in the range of about 40 to 100 theoretical plates.
- the first distillation column is equipped with the means necessary for operation, such as evaporators, condensers, measuring and control devices, connections for the supply and removal of the products, etc.
- the crude aldehyde mixture is generally fed continuously into the middle region (approximately the middle third) of the distillation column, based on the number of theoretical plates.
- the exact point at which the mixture is fed in is not critical, it can be determined by a person skilled in the art using standard methods.
- the distillation conditions in the first distillation column are chosen so that separation into the product streams explained below is achieved.
- the bottom temperature is generally about 1 to 40 ° C., preferably about 10 to 30 ° C., above the boiling point of the straight-chain aldehyde.
- the pressure in the top of the column is generally in the range from 1.0 bar to 1.5 bar (absolute).
- a first aldehyde product stream which is taken off at the top or close to the top of the distillation column as a liquid side draw. It is essentially pure branched aldehyde.
- the branched aldehydes distilled overhead are condensed in a conventional manner, it being possible for part of the condensate to be returned to the column as reflux.
- the reflux ratio is generally in the range from 20 to 30.
- the pure branched aldehyde then leaves the plant. If there are still more volatile constituents in the crude aldehyde mixture than the branched aldehydes, for example carbon monoxide, hydrogen, olefins and paraffins, these are likewise removed overhead and discharged.
- a second aldehyde product stream that is taken directly above or above the evaporator in the area of the first 20% of the total separation stages.
- the second aldehyde product stream is preferably in the region of the first 10% of the total number of theoretical plates, in particular below the first plate, ie. H. taken off directly above the swamp.
- the aldehyde product stream is particularly preferably taken off in vapor form.
- the second aldehyde product stream is essentially a straight-chain aldehyde.
- more than 70% by weight, preferably more than 80% by weight, in particular more than 90% by weight, of the total straight-chain aldehyde present in the crude aldehyde mixture is removed.
- Another high-boiling product stream which is taken off in liquid form at the bottom of the column.
- This product stream contains the above-mentioned high-boiling constituents and 75 to 93% by weight, preferably 80 to 93% by weight, in particular 85 to 93% by weight and particularly preferably 88 to 92% by weight, based on the total weight of the another high-boiling product stream, on straight-chain aldehyde.
- the amount of straight chain aldehyde generally corresponds to about 2 to 5% by weight of the total amount of straight chain aldehyde.
- the further high-boiling product stream iii) is then fed into the middle region of a second (approximately the middle third of the theoretical plates) distillation column. This is smaller than the first distillation column.
- the difference can be expressed by the packing volume, ie the packing volume of the second column is a factor of 50 to 200, preferably 80 to 180, in particular 100 to 170 and particularly preferably 120 to 160 smaller than the packing volume of the first column.
- the ratio of the diameter of the first to the second column is in the range from 10: 1 to 4: 1.
- the column is equipped with the means necessary for operation, such as evaporators, condensers, measuring and control devices, connections for the supply and removal of the products, etc. , fitted.
- the distillation conditions are selected so that a separation into a product stream comprising essentially pure straight-chain aldehyde and a product stream comprising the high boilers is obtained.
- the bottom temperature is generally about 1 to 40 ° C, preferably about 10 to 30 ° C, above the boiling point of the straight-chain aldehyde.
- the pressure in the top of the column is generally in the range from 1.0 bar to 1.5 bar (absolute).
- the pure straight-chain aldehyde is taken off at the top or close to the top of the distillation column, preferably in liquid form, and particularly preferably fed back into the first distillation column above the point at which the product stream ii) is taken off.
- the feed is preferably carried out at approximately the same level as the feed of the crude aldehyde mixture, eg. B. by mixing in the feed of the crude aldehyde mixture.
- essentially all of the straight-chain aldehyde present in the crude aldehyde mixture is obtained as product stream ii).
- the product stream containing the high boilers is withdrawn via the bottom of the second distillation column and leaves the plant.
- the process according to the invention has the advantage that it can be carried out with less effort and under gentle conditions and essentially all of the straight-chain and branched aldehydes are obtained in pure form. Both the straight-chain and the branched aldehydes are obtained in a purity of 99 to 99.98% by weight. In general, the high boiler content in the straight-chain aldehydes is less than 0.5% by weight, in particular less than 0.2% by weight.
- a raw aldehyde mixture of isobutyraldehyde and n-butyraldehyde originating from the hydroformylation and containing 0.01% by weight of lower-boiling components than isobutyraldehyde and 0.5% by weight of higher-boiling components than n-butyraldehyde was used as the starting material.
- the 0 crude aldehyde mixture was as feed 1 with a mass of
- Pure n-butyraldehyde was withdrawn from the column 2 as a gaseous side stream 5 in an amount of about 8,600 kg / h below the first separation stage 5.
- the high-boiling product stream 8 was passed as a bottom draw of approximately 600 kg / h into the second distillation column 9, which was also packed with Mellapak® from Sulzer. Their packing volume was approximately 140 times smaller than that of the first distillation column (diameter ratio
- n-butyraldehyde can be taken off at the top as stream 17, condensed in the condenser 18 and collected in the container 20 and optionally returned to the column 2.
- the bottom draw from column 9 was stream 11 in an amount of approximately
- a crude aldehyde mixture of isobutyraldehyde and n-butyraldehyde with a proportion of 0.01% by weight of lower-boiling constituents than isobutyraldehyde and about 1.3% by weight of higher-boiling constituents than n-butyraldehyde is obtained with a mass of 9,500 kg / h fed as feed 1 to the 58th separation stage of column 2 (same column as in Example 1).
- the distillation takes place at a bottom temperature of column 2 of 98 ° C. and at an absolute top pressure of 1.2 bar.
- Isobutyraldehyde and the low boilers are taken off overhead as stream 13 and condensed in the condenser 14 except for the gaseous components which leave the system as stream 7 (1 kg / h).
- Part of the condensate collected in the container 19 is returned to column 2 as reflux 21 (reflux ratio 30), while pure isobutyraldehyde (about 1400 kg / h) is discharged as stream 3.
- a gaseous side stream 6 from about 7,974 kg / h of pure n-butyraldehyde was removed from column 2 below the 10th separation stage.
- the liquid bottom draw 8 of approximately 600 kg / h is fed into the central region of column 9 (same column as in Example 1).
- the distillation in column 9 is carried out at a bottom temperature of 134 ° C. and at a top pressure of 1.2 bar (absolute). There are 475 kg / h of n-butyraldehyde
- Stream 10 is removed in the top area of the column and returned to the middle area of column 2.
- the bottom draw 11 of the column 9 of approximately 125 kg / h contains the higher-boiling constituents and leaves the plant.
- the purity of the n- and isobutyraldehyde obtained is in each case 99.9% by weight.
- a crude aldehyde mixture of iso-valeraldehyde and n-valeraldehyde with a proportion of 0.2% by weight of lower-boiling components than isovaleraldehyde and about 0.6% by weight of higher-boiling components than n-valeraldehyde is with a mass of 11,000 kg / h as feed 1 to the 58th separation stage of the column (same column as in Example 1).
- the distillation is carried out at a bottom temperature of the column of 120 ° C. and at an absolute top pressure of 1.2 bar.
- Isovaleraldehyde and low boilers are obtained overhead as stream 13 and condensed in the condenser 14 except for the gaseous components which leave the plant as stream 7 (1 kg / h).
- Condensate is returned to column 2 as reflux 21 (reflux ratio 30), while pure isovaleraldehyde (about 1,650 kg / h) leaves the plant as stream 3.
- Pure n-valeraldehyde is taken off as vapor side stream 6 in an amount of about 5 9 279 kg / h below the 10th separation stage of column 2.
- the liquid bottom draw 8 of about 600 kg / h is passed into the middle area of the column 9 (same column as in Example 1).
- the distillation in column 9 takes place at a bottom temperature of 170 ° C. and at a top pressure of 1.2 bar (absolute
- the bottom draw 11 of this column contains at about 70 kg / h the higher-boiling constituents which leave the plant.
- About 530 kg / h of n-valeraldehyde are taken off as stream 10 at the top of column 9 and returned to the middle region of column 2. The purity of the n- and isovaleralde-
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Hydrogen, Water And Hydrids (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
Description
Claims
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP00917005A EP1165480B1 (de) | 1999-03-29 | 2000-03-28 | Verfahren zur destillativen auftrennung eines flüssigen rohaldehydgemisches |
JP2000607961A JP4555483B2 (ja) | 1999-03-29 | 2000-03-28 | 液状の粗製アルデヒド混合物を蒸留により分離する方法 |
DE50003646T DE50003646D1 (de) | 1999-03-29 | 2000-03-28 | Verfahren zur destillativen auftrennung eines flüssigen rohaldehydgemisches |
MXPA01009734A MXPA01009734A (es) | 1999-03-29 | 2000-03-28 | Metodo para separar una mezcla de aldehido crudo liquido mediante destilacion. |
AU38150/00A AU3815000A (en) | 1999-03-29 | 2000-03-28 | Method for separating a liquid crude aldehyde mixture by distillation |
CA002366457A CA2366457C (en) | 1999-03-29 | 2000-03-28 | Method for separating a liquid crude aldehyde mixture by distillation |
AT00917005T ATE249412T1 (de) | 1999-03-29 | 2000-03-28 | Verfahren zur destillativen auftrennung eines flüssigen rohaldehydgemisches |
US09/937,311 US6511583B1 (en) | 1999-03-29 | 2000-10-05 | Method for separating a liquid crude aldehyde mixture by distillation |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19914259.9 | 1999-03-29 | ||
DE19914259A DE19914259A1 (de) | 1999-03-29 | 1999-03-29 | Verfahren zur destillativen Auftrennung eines flüssigen Rohaldehydgemisches |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000058255A1 true WO2000058255A1 (de) | 2000-10-05 |
Family
ID=7902845
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2000/002721 WO2000058255A1 (de) | 1999-03-29 | 2000-03-28 | Verfahren zur destillativen auftrennung eines flüssigen rohaldehydgemisches |
Country Status (13)
Country | Link |
---|---|
US (1) | US6511583B1 (de) |
EP (1) | EP1165480B1 (de) |
JP (1) | JP4555483B2 (de) |
KR (1) | KR100616024B1 (de) |
CN (1) | CN1158236C (de) |
AT (1) | ATE249412T1 (de) |
AU (1) | AU3815000A (de) |
CA (1) | CA2366457C (de) |
DE (2) | DE19914259A1 (de) |
ES (1) | ES2207494T3 (de) |
MX (1) | MXPA01009734A (de) |
MY (1) | MY122741A (de) |
WO (1) | WO2000058255A1 (de) |
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WO2013131936A1 (de) | 2012-03-07 | 2013-09-12 | Basf Se | Verfahren zur wärmeintegration bei der hydrierung und destillation von c3-c20-aldehyden |
US11014863B2 (en) | 2017-05-16 | 2021-05-25 | Basf Se | Hydroformylation method for the large-scale production of aldehydes and/or alcohols |
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WO2016068676A1 (ko) * | 2014-10-31 | 2016-05-06 | 주식회사 엘지화학 | 증류 장치 |
JP6487543B2 (ja) * | 2014-10-31 | 2019-03-20 | エルジー・ケム・リミテッド | 蒸留装置 |
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WO2017182780A1 (en) * | 2016-04-21 | 2017-10-26 | Johnson Matthey Davy Technologies Limited | Process |
TWI784094B (zh) * | 2017-12-01 | 2022-11-21 | 德商贏創運營有限公司 | 自醛獲得醇之方法iii |
CN112299980B (zh) * | 2020-10-10 | 2022-12-27 | 中国神华煤制油化工有限公司 | 混合戊醛分离提纯的方法和系统 |
GB202404300D0 (en) | 2024-03-26 | 2024-05-08 | Johnson Matthey Davy Technologies Ltd | Process for the production of 2-alkylalkanol |
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- 2000-03-28 ES ES00917005T patent/ES2207494T3/es not_active Expired - Lifetime
- 2000-03-28 DE DE50003646T patent/DE50003646D1/de not_active Expired - Lifetime
- 2000-03-28 MX MXPA01009734A patent/MXPA01009734A/es unknown
- 2000-03-28 JP JP2000607961A patent/JP4555483B2/ja not_active Expired - Fee Related
- 2000-03-28 AT AT00917005T patent/ATE249412T1/de not_active IP Right Cessation
- 2000-03-28 CA CA002366457A patent/CA2366457C/en not_active Expired - Fee Related
- 2000-03-28 EP EP00917005A patent/EP1165480B1/de not_active Expired - Lifetime
- 2000-03-28 WO PCT/EP2000/002721 patent/WO2000058255A1/de active IP Right Grant
- 2000-03-28 CN CNB008068968A patent/CN1158236C/zh not_active Expired - Fee Related
- 2000-03-28 KR KR1020017012408A patent/KR100616024B1/ko active IP Right Grant
- 2000-03-28 AU AU38150/00A patent/AU3815000A/en not_active Abandoned
- 2000-10-05 US US09/937,311 patent/US6511583B1/en not_active Expired - Lifetime
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DE3320648A1 (de) * | 1983-06-08 | 1984-12-13 | Ruhrchemie Ag, 4200 Oberhausen | Verfahren zur herstellung von reinem n-butyraldehyd |
EP0216151A2 (de) * | 1985-08-29 | 1987-04-01 | Hoechst Aktiengesellschaft | Verfahren zur Herstellung von 2-Ethylhexanol |
EP0484977A2 (de) * | 1990-11-09 | 1992-05-13 | Union Carbide Chemicals And Plastics Company, Inc. | Trennung von Aldehydgemischen |
US5227544A (en) * | 1991-02-15 | 1993-07-13 | Basf Corporation | Process for the production of 2-ethylhexanol |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
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CN102580337A (zh) * | 2012-01-19 | 2012-07-18 | 天津大学 | 混合丁醛分离装置及填料塔的应用 |
WO2013131936A1 (de) | 2012-03-07 | 2013-09-12 | Basf Se | Verfahren zur wärmeintegration bei der hydrierung und destillation von c3-c20-aldehyden |
US11769597B2 (en) | 2015-12-03 | 2023-09-26 | Regeneron Pharmaceuticals, Inc. | Methods of associating genetic variants with a clinical outcome in patients suffering from age-related macular degeneration treated with anti-VEGF |
US11014863B2 (en) | 2017-05-16 | 2021-05-25 | Basf Se | Hydroformylation method for the large-scale production of aldehydes and/or alcohols |
US11519020B2 (en) | 2018-05-25 | 2022-12-06 | Regeneron Pharmaceuticals, Inc. | Methods of associating genetic variants with a clinical outcome in patients suffering from age-related macular degeneration treated with anti-VEGF |
Also Published As
Publication number | Publication date |
---|---|
DE50003646D1 (de) | 2003-10-16 |
CN1158236C (zh) | 2004-07-21 |
KR100616024B1 (ko) | 2006-08-28 |
ATE249412T1 (de) | 2003-09-15 |
US6511583B1 (en) | 2003-01-28 |
EP1165480A1 (de) | 2002-01-02 |
DE19914259A1 (de) | 2000-10-05 |
AU3815000A (en) | 2000-10-16 |
MXPA01009734A (es) | 2002-03-27 |
CA2366457A1 (en) | 2000-10-05 |
KR20010105400A (ko) | 2001-11-28 |
JP4555483B2 (ja) | 2010-09-29 |
CA2366457C (en) | 2008-05-06 |
ES2207494T3 (es) | 2004-06-01 |
JP2002540181A (ja) | 2002-11-26 |
CN1349487A (zh) | 2002-05-15 |
EP1165480B1 (de) | 2003-09-10 |
MY122741A (en) | 2006-05-31 |
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