公开(公告)号：JP2011006411A

公开(公告)日：2011-01-13

申请号：JP2010140108

申请日：2010-06-21

Applicant: Basf Se ,  ビーエーエスエフ ソシエタス・ヨーロピアBasf Se

Inventor： KAIBEL GERD DR ,  MUELLER CHRISTIAN ,  HUGO RANDOLF ,  HEIDA BERND

IPC: C07C7/04 ,  B01D3/32 ,  C07C7/08 ,  C07C9/08 ,  C07C9/10 ,  C07C11/06 ,  C07C11/08 ,  C07C11/167

CPC classification number: B01D3/14 ,  B01D3/141 ,  B01D3/32 ,  C07C7/08 ,  C07C11/06 ,  C07C11/167

Abstract: PROBLEM TO BE SOLVED: To provide a method wherein processings are integrated by separating mixtures into two fractions by distillation to thereby reduce costs of capital.SOLUTION: There is provided a method for separating one or more feed mixtures by distillation in a column having one, two, or three partition walls which continue in longitudinal direction of the column from one end to the other end of the column and partition the interior of the column into two, three, or four completely separate column subregions by using a liquid-phase flow from a first column subregion into a second column subregion, optionally a third column subregion, and optionally a fourth column subregion and in countercurrent to a flow of vapor, wherein the one or more feed mixtures are separated into two fractions in the column and the column has a single bottom vaporizer and a single condenser at the top of the column.

Abstract translation: 要解决的问题：提供一种方法，其中通过蒸馏将混合物分离成两个馏分来整合处理，从而降低资本成本。解决方案：提供了一种通过蒸馏在一个塔中分离一种或多种进料混合物的方法， 两个或三个分隔壁，其从塔的纵向方向延伸到柱的一端到另一端，并且通过使用液相流从塔的内部将柱的内部分隔成两个，三个或四个完全分离的柱子区域 第一列子区域，第二列子区域，可选地第三列子区域，以及可选地第四列子区域，并且与蒸汽流逆流，其中一个或多个进料混合物在塔中分成两部分， 单塔底部蒸发器和柱顶部的单个冷凝器。

公开(公告)号：JP2010284645A

公开(公告)日：2010-12-24

申请号：JP2010131648

申请日：2010-06-09

Applicant: Basf Se ,  ビーエーエスエフ ソシエタス・ヨーロピアBasf Se

Inventor： KAIBEL GERD DR ,  HEIDA BERND ,  HUGO RANDOLF

IPC: B01D3/40 ,  B01D3/16 ,  B01J19/32 ,  C07C7/08 ,  C07C9/10 ,  C07C11/08 ,  C07C11/167 ,  C07C11/18

CPC classification number: B01J19/32 ,  B01D3/40 ,  B01D3/42 ,  B01J2219/3221 ,  B01J2219/32213 ,  B01J2219/32227 ,  B01J2219/32258

Abstract: PROBLEM TO BE SOLVED: To provide a method for separating a certain substance from a mixture including the certain substance by distillation.
SOLUTION: A structured packing material having one or more residence layers whose specific surface areas are equal to or higher than a flooding point in one or more residence layers 1, and one or more separation layers 2 whose specific surface areas are lower than the flooding point, is used in a distillation column as a packing material having an excellent separating effect in order to execute the method of separation by distillation for separating the certain substance from the mixture including the certain substance by adding a selective solvent and using extractive distillation.
COPYRIGHT: (C)2011,JPO&INPIT

Abstract translation: 待解决的问题：提供一种通过蒸馏从某种物质的混合物中分离某种物质的方法。 解决方案：具有一个或多个比表面积等于或高于一个或多个停留层1中的溢流点的一个或多个停留层以及一个或多个比表面积低于 淹水点用作蒸馏塔作为具有优异分离效果的包装材料，以便通过蒸馏分离特定物质从包括某些物质的混合物中分离的方法，通过加入选择性溶剂并使用萃取蒸馏 。 版权所有（C）2011，JPO＆INPIT

公开(公告)号：WO2011054798A3

公开(公告)日：2011-07-21

申请号：PCT/EP2010066595

申请日：2010-11-02

Applicant: BASF SE ,  HUGO RANDOLF ,  PESCHEL WERNER ,  STABEL UWE ,  ZACHMANN HARRY ,  JAEGER MICHAEL

Inventor： HUGO RANDOLF ,  PESCHEL WERNER ,  STABEL UWE ,  ZACHMANN HARRY ,  JAEGER MICHAEL

IPC: C07C7/08 ,  C07C11/167 ,  C10G7/08

CPC classification number: C10G21/20 ,  B01D3/40 ,  C07C7/08 ,  C10G7/08 ,  C10G2300/44 ,  C07C11/167

Abstract: A method is provided for separating a C4 fraction (2) by means of extractive distillation using a selective solvent (1) by way of counter-flow of the C4 fraction (2) and of the selective solvent (1) in a liquid phase in a distillation unit (K I, K II), while separating a head flow (3) comprising the butanes and butenes from the C4 fraction and a bottom flow (6) comprising the selective solvent and the remaining components of the C4 fraction, with the exception of the butanes and butenes, the selective solvent being outgased from the fraction in an additional step, characterized in that energy is extracted from the distillation unit (K I, K II) between the extraction point for the head flow (3) and the extraction point for the bottom flow (6).

Abstract translation: 公开了一种用于使用选择性溶剂（2）通过萃取蒸馏分馏C4馏分的处理（1）由C 4馏分（2）的逆流流动和选择性溶剂（1）在蒸馏单元中的液相（KI，K II） 并除去含有丁烷和从C4馏分的丁烯和（6）含有所述选择性溶剂的塔底物流和除丁烷和丁烯的C 4馏分的其余部件的顶部料流（3）的，从在 进一步的工艺步骤脱气选择性溶剂，其在取出点之间，其特征在于，用于所述塔顶物流（3）和用于底部料流（6）能量从蒸馏单元（KI，K II）取出点被抽出。

公开(公告)号：WO2013050367A2

公开(公告)日：2013-04-11

申请号：PCT/EP2012069458

申请日：2012-10-02

Applicant: BASF SE ,  SCHAUB THOMAS ,  BEY OLIVER ,  MEIER ANTON ,  FRIES DONATA MARIA ,  HUGO RANDOLF

Inventor： SCHAUB THOMAS ,  BEY OLIVER ,  MEIER ANTON ,  FRIES DONATA MARIA ,  HUGO RANDOLF

IPC: C07C51/02

CPC classification number: C07C51/02 ,  B01J31/0202 ,  B01J31/0237 ,  B01J31/24 ,  B01J31/2414 ,  B01J2231/625 ,  B01J2531/821 ,  B01J2531/98 ,  C07C51/41 ,  C07C51/48 ,  C07C53/02 ,  C07C53/06

Abstract: The invention relates to a method for producing formic acid, comprising the following steps: (a) reacting, in a homogeneously catalyzed manner, a reaction mixture (Rg) containing carbon dioxide, hydrogen, at least one polar solvent selected from the group comprising methanol, ethanol, 1-propanol, 2-propanol, 1-butanol, 2-butanol, 2-methyl-1-propanol, and water, and at least one tertiary amine of general formula (A1) NR1R2R3, in which R1, R2, and R3 represent independently of one another an unbranched or branched, acyclic or cyclic, aliphatic, araliphatic, or aromatic group having 1 to 16 carbon atoms, wherein individual carbon atoms can also be substituted independently of one another with a hetero group selected from the groups -O- and >N- and two or all three residues can also be bonded to one another to from a chain comprising at least four atoms, in the presence of at least one coordination catalyst, which contains at least one element selected from groups 8, 9, and 10 of the periodic system, in a hydrogenation reactor in order to obtain, optionally after adding water, a two-phase hydrogenation mixture (H) containing an upper phase (O1), which contains the at least one coordination catalyst and the at least one tertiary amine (A1), and a lower phase (U1), which contains the at least one polar solvent, residues of the at least one coordination catalyst, and at least one formic acid/amine adduct of general formula (A2), NR1R2R3 * xi HCOOH, in which xi is in the range of 0.4 to 5 and R1, R2, R3 have the meanings stated above; (b) processing the hydrogenation mixture (H) obtained in step (a) according to one of the following steps: (b1) phase-separating the hydrogenation mixture (H) obtained in step (a) in a first phase-separating device into the upper phase (O1) and the lower phase (U1), or (b2) extracting the at least one coordination catalyst from the hydrogenation mixture (H) obtained in step (a) in an extraction unit with an extracting agent containing the at least one tertiary amine (A1) in order to obtain a raffinate (R1) containing the at least one formic acid/amine adduct (A2) and the at least one polar solvent and an extract (E1) containing the at least one tertiary amine (A1) and the at least one coordination catalyst, or (b3) phase-separating the hydrogenation mixture (H) obtained in step (a) in a first phase-separating device into the upper phase (O1) and the lower phase (U1) and extracting the residues of the at least one coordination catalyst from the lower phase (U1) in an extraction unit by means of an extracting agent containing the at least one tertiary amine (A1) in order to obtain a raffinate (R2) containing the at least one formic acid/amine adduct (A2) and the at least one polar solvent and an extract (E2) containing the at least one tertiary amine (A1) and the residues of the at least one coordination catalyst; (c) separating the at least one polar solvent from the lower phase (U1), from the raffinate (R1), or from the raffinate (R2) in a first distillation device in order to obtain a distillate (D1) containing the at least one polar solvent, which is fed back into the hydrogenation reactor in step (a), and a two-phase bottom mixture (S1) containing an upper phase (O2), which contains the at least one tertiary amine (A1), and a lower phase (U2), which contains the at least one formic acid/amine adduct (A2); (d) optionally processing the bottom mixture (S1) obtained in step (c) by phase separation in a second phase-separating device into the upper phase (O2) and the lower phase (U2); (e) cleaving the at least one formic acid/amine adduct (A2) contained in the bottom mixture (S1) or optionally in the lower phase (U2) in a thermal cleaving unit in order to obtain the at least one tertiary amine (A1), which is fed back to the hydrogenation reactor in step (a), and formic acid, which is discharged from the thermal cleaving unit, wherein carbon monoxide is added to the lower phase (U1), the raffinate (R1), or the raffinate (R2) directly before and/or during step (c) and/or carbon monoxide is added to the bottom mixture (S1) or optionally the bottom phase (U2) directly before and/or during step (e).

Abstract translation: 本发明涉及一种用于生产甲酸的方法，包括以下步骤：（a）均匀催化的反应混合物的反应含有二氧化碳，氢气，选自甲醇，乙醇，1-丙醇组成的组中选择的至少一种极性溶剂，2（RG） 丙醇，1-丁醇，2-丁醇，2-甲基-1-丙醇和水，并且所述通式（A1）NR1R2R3中的至少一种叔胺，其中R1，R2，R3彼此独立地，无支链的或支链的，无环或环状 代表脂族，芳脂族或芳族基具有在每种情况下为1〜16个碳原子，其特征在于，单独的碳原子可以被选自组中选择的杂原子基团-O-和> N-取代，以及两个独立地或所有三个基团，以形成至少四个 包含链原子可一起还可以连接在至少一个Komplexkatalysato的存在 含选自8,9和在氢化反应器含有上层相周期表的第10选择的至少一种元素RS获得的，如果适当添加WASER后，对应于所述至少一个配位化合物催化剂的两相加氢混合物（H）（01）和 包含所述至少一种极性溶剂中的至少一种叔胺（A1），和下部相（U1）中，至少一个配位化合物催化剂和通式中的至少一种甲酸 - 胺加合物（A2）的残基，NR1R2R3 * XI HCOOH， xi是在从0.4到5的范围内，R1，R2，R3具有以上给出的含义，（一）（H）根据相分离的下面（b1）的一个获得的氢化混合物（b）的后处理步骤 步骤（a）获得在上部相（O1）第一相分离器氢化混合物（H）和下层相（U1）或（b2）提取从所述至少一个配合物催化剂 在步骤氢化混合物（a）中获得（H）在萃取单元用含有包含至少一个甲酸 - 胺加合物（A2）和所述至少一种极性溶剂中的至少一种叔胺（A1），以获得萃余液（R1）的提取剂 和含有至少一种叔胺（A1）和所述至少一个配合物催化剂或在步骤（b3）中的相分离的提取物氢化混合物（E1）（a）以在上部相（O1）的第一相分离器和下部相中获得（H）（ U1），并用含有包含至少一个甲酸 - 胺加合物的至少一种叔胺（A1），以获得萃余液（R2）萃取剂从下部相（D1）至少一种配合物催化剂在提取单元中的残基的提取（A2） 和所述至少一种极性溶剂和含有至少一种叔胺（A1）和RES的提取物（E2） 所述至少一个配合物催化剂的叔，（c）从所述提余液（R1）或者从在第一蒸馏装置的提余液（R2）分离下层相（U1）的所述至少一种极性溶剂，得到含有至少一种馏出物（D1） 中相应的氢化反应器中在步骤（a）再循环极性溶剂，和包含含有至少一种叔胺（A1）的上层相（O 2），和下部相（U2），其是至少两相塔底混合物（S1） 包含甲酸 - 胺加合物（A2），（d）任选地，在后处理步骤（c）中获得通过相分离产物塔底混合物（S1）在第二相分离器进入上部相（O 2）和下层相（U2），（e）中裂解 在底部（S1）（U2）的混合物，并且如果合适，在下层相包含在热裂解单元的至少一种甲酸 - 胺加合物（A2），以获得所述至少一个 叔胺（A1），其中（a）再循环到在步骤氢化反应器，以及甲酸，其从该热裂解单元放电，之前和/或期间，步骤（c）的下部相（U1）中，萃余液（R1 ）或提余液（R2），一氧化碳被添加和/或直接之前和/或期间，步骤（e）的底部混合物（S1）和，如果合适的话，下层相（U2），一氧化碳加入。

公开(公告)号：WO2008104582A2

公开(公告)日：2008-09-04

申请号：PCT/EP2008052413

申请日：2008-02-28

Applicant: BASF SE ,  DAHMEN KIRSTEN ,  OFTRING ALFRED ,  BAUMANN KATRIN ,  HUGO RANDOLF ,  HAHN THILO ,  MELDER JOHANN-PETER

Inventor： DAHMEN KIRSTEN ,  OFTRING ALFRED ,  BAUMANN KATRIN ,  HUGO RANDOLF ,  HAHN THILO ,  MELDER JOHANN-PETER

IPC: C07C211/14 ,  C07C209/48 ,  C07C253/00 ,  C07D295/13

CPC classification number: C07D295/13

Abstract: The invention relates to a method for producing triethylenetetramine (TETA), comprising the following steps: a) ethylenediamine (EDA) is reacted with formaldehyde and hydrogen cyanide (HCN), the molar ratio of EDA to formaldehyde to HCN being between 1 : 1.5 : 1.5 and 1 : 2 : 2 [mol/mol/mol], to obtain ethylenediamine diacetonitrile (EDDN); b) the EDDN obtained in step a) is hydrogenated in the presence of a catalyst and a solvent.

Abstract translation: 本发明涉及一种制备三亚乙基四胺（TETA），包括以下步骤：a）乙烯二胺（EDA）与甲醛和氰化氢（HCN），反应，其中EDA的甲醛给HCN摩尔比1：1.5：1 ，最高达1 5：2：2 [摩尔/摩尔/摩尔]是给乙二胺二（EDDN）中，b）在步骤所获得的氢化）EDDN的在催化剂和溶剂的存在下进行。

公开(公告)号：PL2545019T3

公开(公告)日：2014-08-29

申请号：PL11709361

申请日：2011-03-08

Applicant: BASF SE

Inventor： HEIDA BERND ,  HUGO RANDOLF

IPC: C07C7/08 ,  B01D3/40 ,  C07C11/167

公开(公告)号：CA2851175A1

公开(公告)日：2013-04-11

申请号：CA2851175

申请日：2012-10-02

Applicant: BASF SE

Inventor： SCHAUB THOMAS ,  BEY OLIVER ,  MEIER ANTON ,  FRIES DONATA MARIA ,  HUGO RANDOLF

IPC: C07C51/02 ,  C07C51/42 ,  C07C53/02

Abstract: The invention relates to a method for producing formic acid, comprising the following steps: (a) reacting, in a homogeneously catalyzed manner, a reaction mixture (Rg) containing carbon dioxide, hydrogen, at least one polar solvent and at least one tertiary amine in the presence of at least one coordination catalyst in a hydrogenation reactor in order to obtain a two-phase hydrogenation mixture (H) containing an upper phase (O1), which contains the at least one coordination catalyst and the at least one tertiary amine (A1), and a lower phase (U1), which contains the at least one polar solvent, residues of the at least one coordination catalyst, and at least one formic acid/amine adduct; (b) processing the hydrogenation mixture (H) obtained in step (a) according to one of the following steps: (b1) phase-separating the hydrogenation mixture (H) obtained in step (a) in a first phase-separating device into the upper phase (O1) and the lower phase (U1), or (b2) extracting the at least one coordination catalyst from the hydrogenation mixture (H) obtained in step (a) in an extraction unit with an extracting agent containing the at least one tertiary amine (A1) in order to obtain a raffinate (R1) containing the at least one formic acid/amine adduct (A2) and the at least one polar solvent and an extract (E1) containing the at least one tertiary amine (A1) and the at least one coordination catalyst, or (b3) phase-separating the hydrogenation mixture (H) obtained in step (a) in a first phase-separating device into the upper phase (O1) and the lower phase (U1) and extracting the residues of the at least one coordination catalyst from the lower phase (U1) in an extraction unit by means of an extracting agent containing the at least one tertiary amine (A1) in order to obtain a raffinate (R2) containing the at least one formic acid/amine adduct (A2) and the at least one polar solvent and an extract (E2) containing the at least one tertiary amine (A1) and the residues of the at least one coordination catalyst; (c) separating the at least one polar solvent from the lower phase (U1), from the raffinate (R1), or from the raffinate (R2) in a first distillation device in order to obtain a distillate (D1) containing the at least one polar solvent, which is fed back into the hydrogenation reactor in step (a), and a two-phase bottom mixture (S1) containing an upper phase (O2), which contains the at least one tertiary amine (A1), and a lower phase (U2), which contains the at least one formic acid/amine adduct (A2); (e) cleaving the at least one formic acid/amine adduct (A2) contained in the bottom mixture (S1) or optionally in the lower phase (U2) in a thermal cleaving unit in order to obtain the at least one tertiary amine (A1), which is fed back to the hydrogenation reactor in step (a), and formic acid, which is discharged from the thermal cleaving unit, wherein carbon monoxide is added to the lower phase (U1), the raffinate (R1), or the raffinate (R2) directly before and/or during step (c) and/or carbon monoxide is added to the bottom mixture (S1) or optionally the bottom phase (U2) directly before and/or during step (e).

公开(公告)号：AT524429T

公开(公告)日：2011-09-15

申请号：AT06778022

申请日：2006-07-27

Applicant: BASF SE

Inventor： HUGO RANDOLF ,  DAHMEN KIRSTEN ,  HUBER SABINE

IPC: C07C209/48 ,  C07C211/27

Abstract: Processes for preparing a xylylenediamine by continuous hydrogenation, wherein the processes comprise: introducing a liquid circulation stream comprising a phthalonitrile and ammonia into a reactor to continuously hydrogenate the phthalonitrile in the presence of a heterogenous catalyst and the ammonia such that a reactor effluent comprising the xylylenediamine is formed; drawing off a portion of the reactor effluent to provide a first recycle stream; mixing at least a portion of the first recycle stream in a mixing unit with liquid ammonia and fresh phthalonitrile in solid or molten form to provide a second recycle stream; and recycling the second recycle stream to the liquid circulation stream, or wherein the second recycle stream and any remaining unmixed portion of the first recycle stream are both recycled to the liquid circulation stream.

公开(公告)号：AU2007216457B2

公开(公告)日：2011-02-24

申请号：AU2007216457

申请日：2007-02-14

Applicant: BASF SE

Inventor： HUGO RANDOLF ,  WAGNER RUPERT

IPC: B01D53/14 ,  C10L3/10

Abstract: In a method for removing acid gases from a fluid stream, the fluid stream, which is in contact with an absorption medium within an absorber, is passed through a first absorption zone in the absorber to remove a majority of acid gases from the fluid stream. The fluid stream is susequently passed through a second absorption zone in the absorber to further remove acid gases from the fluid stream. The loaded absorption medium is passed into a first regeneration zone to obtain a partially regenerated absorption medium, and a part of the partially regenerated absorption medium is passed into the first absorption zone. The other part of the partially regenerated absorption medium is passed into a second regeneration zone to obtain a regenerated absorption medium. A part of the regenerated absorption medium is passed into the first absorption zone and the other part is passed into the second absorption zone.

公开(公告)号：IN3122DEN2014A

公开(公告)日：2015-05-22

申请号：IN3122DEN2014

申请日：2014-04-21

Applicant: BASF SE

Inventor： SCHAUB THOMAS ,  BEY OLIVER ,  MEIER ANTON ,  FRIES DONATA MARIA ,  HUGO RANDOLF

IPC: C07C51/00 ,  C07C51/02 ,  C07C51/42

Abstract: The invention relates to a method for producing formic acid comprising the following steps: (a) reacting in a homogeneously catalyzed manner a reaction mixture (Rg) containing carbon dioxide hydrogen at least one polar solvent and at least one tertiary amine in the presence of at least one coordination catalyst in a hydrogenation reactor in order to obtain a two phase hydrogenation mixture (H) containing an upper phase (O1) which contains the at least one coordination catalyst and the at least one tertiary amine (A1) and a lower phase (U1) which contains the at least one polar solvent residues of the at least one coordination catalyst and at least one formic acid/amine adduct; (b) processing the hydrogenation mixture (H) obtained in step (a) according to one of the following steps: (b1) phase separating the hydrogenation mixture (H) obtained in step (a) in a first phase separating device into the upper phase (O1) and the lower phase (U1) or (b2) extracting the at least one coordination catalyst from the hydrogenation mixture (H) obtained in step (a) in an extraction unit with an extracting agent containing the at least one tertiary amine (A1) in order to obtain a raffinate (R1) containing the at least one formic acid/amine adduct (A2) and the at least one polar solvent and an extract (E1) containing the at least one tertiary amine (A1) and the at least one coordination catalyst or (b3) phase separating the hydrogenation mixture (H) obtained in step (a) in a first phase separating device into the upper phase (O1) and the lower phase (U1) and extracting the residues of the at least one coordination catalyst from the lower phase (U1) in an extraction unit by means of an extracting agent containing the at least one tertiary amine (A1) in order to obtain a raffinate (R2) containing the at least one formic acid/amine adduct (A2) and the at least one polar solvent and an extract (E2) containing the at least one tertiary amine (A1) and the residues of the at least one coordination catalyst; (c) separating the at least one polar solvent from the lower phase (U1) from the raffinate (R1) or from the raffinate (R2) in a first distillation device in order to obtain a distillate (D1) containing the at least one polar solvent which is fed back into the hydrogenation reactor in step (a) and a two phase bottom mixture (S1) containing an upper phase (O2) which contains the at least one tertiary amine (A1) and a lower phase (U2) which contains the at least one formic acid/amine adduct (A2); (e) cleaving the at least one formic acid/amine adduct (A2) contained in the bottom mixture (S1) or optionally in the lower phase (U2) in a thermal cleaving unit in order to obtain the at least one tertiary amine (A1) which is fed back to the hydrogenation reactor in step (a) and formic acid which is discharged from the thermal cleaving unit wherein carbon monoxide is added to the lower phase (U1) the raffinate (R1) or the raffinate (R2) directly before and/or during step (c) and/or carbon monoxide is added to the bottom mixture (S1) or optionally the bottom phase (U2) directly before and/or during step (e).