公开(公告)号：AT409680T

公开(公告)日：2008-10-15

申请号：AT05821923

申请日：2005-12-19

Applicant: BASF SE

Inventor： CRONE SVEN ,  KLANNER CATHARINA ,  SCHINDLER GOETZ-PETER ,  DUDA MARK ,  BORGMEIER FRIEDER

IPC: C07C5/333 ,  C07C11/167

Abstract: A process for preparing butadiene, comprising nonoxidatively dehydrogenating n-butane from a stream (a) in a first dehydrogenation zone to obtain stream (b) comprising 1-butene, 2-butene, and butadiene; oxidatively dehydrogenating the 1-butene and 2-butene of (b) in the presence of an oxygenous gas in a second dehydrogenation zone to obtain stream (c) comprising n-butane, butadiene, hydrogen, and steam; compressing and cooling (c) to obtain stream (d2) comprising n-butane, butadiene, hydrogen, and steam; extractively distilling (d2) into stream (e1) comprising butadiene and stream (e2) comprising n-butane, hydrogen, and steam; optionally compressing and cooling (e2) to obtain stream (f1) comprising n-butane and water and stream (f2) comprising n-butane and hydrogen and optionally recycling (f1) into the first dehydrogenation zone; separating (f2) into stream (g1) comprising n-butane and stream (g2) comprising hydrogen by contacting (f2) with a high boiling absorbent and subsequently desorbing the gas constituents dissolved in the absorbent.

公开(公告)号：AU2007233921A1

公开(公告)日：2007-10-11

申请号：AU2007233921

申请日：2007-03-13

Applicant: BASF SE

Inventor： SIMON FALK ,  MULLER ULRICH ,  SCHUBERT MARKUS ,  KIENER CHRISTOPH ,  CRONE SVEN ,  TEICH FRIEDHELM ,  PASTRE JORG

IPC: C07C7/12 ,  C07C7/13

Abstract: The present invention relates to processes for preparing propene from propane, comprising the steps: A) a feed gas stream a comprising propane is provided; B) the feed gas stream a comprising propane, if appropriate steam and if appropriate and an oxygenous gas stream are fed into a dehydrogenation zone and propane is subjected to a dehydrogenation to propene to obtain a product gas stream b comprising propane, propene, methane, ethane, ethene, hydrogen, if appropriate carbon monoxide, carbon dioxide, steam and oxygen; C) the product gas stream b is cooled, if appropriate compressed and steam is removed by condensation to obtain a steam-depleted product gas stream c; D) the product gas stream c is contacted with a selective adsorbent which adsorbs propene selectively under the selected adsorption conditions to obtain a propene-laden adsorbent and a propene-depleted gas stream d2 comprising propane, methane, ethane, ethene and hydrogen, carbon monoxide and carbon dioxide; E) a propene-comprising gas stream e1 is released from the propane-laden adsorbent by pressure reduction and/or heating of the adsorbent.

公开(公告)号：EA036481B1

公开(公告)日：2020-11-16

申请号：EA201790647

申请日：2014-10-09

Applicant: BASF SE

Inventor： WAGNER HANS-GUENTER ,  BAYER CHRISTOPH ,  KARRER LOTHAR ,  RUETTER HEINZ ,  PIETZ PATRIK ,  CRONE SVEN ,  EGGERSMANN MARKUS ,  WONG KAM WING ,  KIRCHNER GUENTHER ,  ZIMMER GABRIELE

IPC: B01J20/34

Abstract: Изобретениеотноситсяк способурегенерацииадсорбера (A) путемконтактас потоком (S1), прикоторомпоток (S1) нагреваютпредварительно, какминимум, двумятеплообменнымиблоками (ТОБ1) и (ТОБ2). Вкачествевыходящегоизадсорбера (A) потокаполучаютпоток (S2), которыйпроходитчерез, какминимум, дватеплообменныхблока (ТОБ1) и (ТОБ2), пересекаемыепотоком (S1), прикоторомтемпературапотока (S2), питающегокаждыйтеплообменныйблок, вышечемтемпературапотока (S1), питающеготеплообменныеблоки (ТОБ1) и (ТОБ2), длятогочтобынепосредственнопереноситьтеплоотпотока (S2) напоток (S1).

公开(公告)号：EA033611B1

公开(公告)日：2019-11-08

申请号：EA201790703

申请日：2014-10-09

Applicant: BASF SE

Inventor： WAGNER HANS-GUENTER ,  BAYER CHRISTOPH ,  KARRER LOTHAR ,  EGGERSMANN MARKUS ,  CRONE SVEN ,  WONG KAM WING ,  RUETTER HEINZ ,  PIETZ PATRIK

IPC: C10G25/00 ,  B01D53/04 ,  C07B63/00 ,  C10G25/12

Abstract: Изобретениеотноситсяк способуочисткиорганическойкомпозиции (OC1) путемадсорбциис использованиемагрегата, содержащегокакминимумдваадсорбера. Органическойкомпозицией (OC1), содержащейкакминимумодиналкан, какминимумодинолефини какминимумодносоединение, содержащеекислороди/илисеру, питаютпервыйадсорбер (А1) агрегатадлятого, чтобыполучитьорганическуюкомпозицию (OC2), содержащуюкакминимумодиналкан, какминимумодинолефини уменьшенноеколичествокакминимумодногосоединения, содержащегокислороди/илисеру, посравнениюс соответствующимколичествомв органическойкомпозиции (OC1). Врезультатегидрированияорганическойкомпозиции (OC2) получаютпоток (S2), содержащийкакминимумодиналкани уменьшенноеколичествокакминимумодногоолефинапосравнениюс соответствующимколичествомв органическойкомпозиции (OC2), полученнойпослепитанияпервогоадсорбера (А1). Второйадсорбер (А2) агрегатарегенерируютпутемконтактас потоком (S2).

公开(公告)号：IN1057MUN2014A

公开(公告)日：2015-05-01

申请号：IN1057MUN2014

申请日：2014-05-30

Applicant: BASF SE

Inventor： CRONE SVEN ,  RYLL OLIVER ,  BLUM TILL ,  WECK ALEXANDER ,  PAPP RAINER ,  KROKOSZINSKI ROLAND ,  BLANKERTZ HEINRICH JOSEF

IPC: C07C2/10 ,  C07C11/02

Abstract: Procedure for manufacturing oligomers by continuous oligomerization of butenes characterized in that a) an initial stream is used which contains 1 butene and 2 butene at a total concentration of 10 to 70 wt% and 10 to 60 wt% of iso butane (called initial stream 1 hereafter) b) said initial stream 1 is converted until more than 60 wt% of the 1 butene contained in initial stream 1 but less than 50 wt% of the 2 butene contained in initial stream 1 are converted into oligomers c) the oligomers obtained in b) are separated and optionally fed to further processing and the remaining stream is fed to a distillation processing step d) iso butane is separated by distillation from the remaining steam e) the iso butane depleted stream (called initial stream 2 hereafter) obtained after the distillation processing step d) is converted into oligomers.

公开(公告)号：ES2454693T3

公开(公告)日：2014-04-11

申请号：ES06792911

申请日：2006-08-21

Applicant: BASF SE

Inventor： VAN LAAR FREDERIK ,  SCHWAB EKKEHARD ,  VOSS HARTWIG ,  ANDERS JOACHIM-THIERRY ,  CRONE SVEN ,  MACKENROTH WOLFGANG

IPC: C07C209/02 ,  B01D53/22 ,  B01D67/00 ,  B01D69/00 ,  B01D69/02 ,  B01D69/10 ,  B01D71/02 ,  C01B3/50 ,  C07C211/46

Abstract: Procedimiento para la fabricación de anilina, caracterizado porque una mezcla de reacción, en la que benceno y amoniaco se alimentan separada o conjuntamente, se conduce en un circuito que presenta un reactor de membrana con catalizador y separación de hidrógeno integrada a través de una membrana permeable al hidrógeno, porque se elimina hidrógeno de la mezcla de reacción a través de la membrana permeable al hidrógeno, separando la membrana el lado de rechazo (lado de la reacción) del lado del permeado y llegando el hidrógeno formado en el lado del rechazo a través de la membrana al lado del permeado, donde el hidrógeno se elimina por reacción y/o transporte de materia, y la presión de la mezcla de reacción que contiene benceno y amoniaco en presencia de catalizador en el reactor de membrana asciende a entre 1 y 15 MPa, y se retira anilina del circuito.

公开(公告)号：BRPI0718526A2

公开(公告)日：2013-11-12

申请号：BRPI0718526

申请日：2007-12-17

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

IPC: B01F5/04 ,  B01J8/08 ,  B01J8/12 ,  C07C5/32

Abstract: The reactor (1) for continuous oxide hydrogenation of a feed gas flow (2) of saturated hydrocarbons, which are previously mixed with a gas flow (3) containing oxygen, on a moving catalyst bed (4) arranged between two concentric cylindrical holding devices (5, 6) in the longitudinal direction of the reactor by leaving a central inner space and an intermediate space, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating disk-type deflector plates arranged in the central inner space. The reactor (1) for a continuous oxide hydrogenation of a feed gas flow (2) of saturated hydrocarbons, which are previously mixed with a gas flow (3) containing oxygen, on a moving catalyst bed (4) arranged between two concentric cylindrical holding devices (5, 6) in the longitudinal direction of the reactor by leaving a central inner space and an intermediate space between the moving catalyst bed and an inner envelope of the reactor to obtain a reaction gas mixture, comprises four reactor sections, which are separated from each other and split into sub-sections by alternating disk-type deflector plates arranged in the central inner space, and annular deflector plates arranged in the intermediate space between the moving catalyst bed and the inner envelope of the reactor. Each reactor sections comprise a mixing device, which is arranged in the direction of flow of the reaction gas mixture upstream of the moving catalyst bed. The mixing device is formed from two or three successively arranged rows of tubes having turbulence generators on the outer side of the tubes, which narrow the cross-section for the passage of the feed gas flow to 1/3-1/6 of the free cross-section. The oxygen-containing gas flow is guided through the tubes and sprayed into the feed gas flow through holes in the tubes in addition to a perforated plate mounted upstream of the tubes and a further perforated plate mounted downstream of the tubes. The tubes are ribbed tubes with the turbulence generators. The holes in rib gears are arranged between the ribs of the ribbed tubes. The ribbed tubes have 100-300 circulations of the ribs per meter length of the ribbed tubes, are formed from tubes with cylindrical outer circumference and are welded in spiral-shaped manner on the outer circumference along a strip longitudinal edge from a longitudinal strip containing ribs, which are notched under the formation of segments with exception of a rib base. An outer diameter of the tubes is 20-50 mm. A ratio of the height of the ribs to the outer diameter of the tubes is 1/10:1/2. The segments are distorted against the rib base in an angle. A thickness of the ribs is 0.3-1.5 mm and a width of the segments is 4-8 mm. The second row of the ribbed tubes is arranged in a gap to the first row of the ribbed tubes. The third row of the ribbed tubes is arranged in a gap to the second row of the ribbed tubes. The diameter of the holes in the upstream perforated plate is smaller than the half of the small distance of the ribs between two sequential circulations on each other. A ratio of the perforated plate thickness to the diameter of the holes in the perforated plate is 0.75:2.0. The diameter of the holes in the downstream perforated plate is larger or same to the diameter of the holes in the upstream perforated plate. The upstream perforated plate is arranged in a distance to flowing level of the first row of the ribbed tubes through the feed gas flow according to 7-20 times of the diameter of the holes in the upstream perforated plate. Two holes per rib gear are arranged between the ribs at diametrically opposite positions of the rib gears with small distance to the adjacent ribbed tubes in the row of the ribbed tubes. A ratio of the holes in the upstream perforated plate is defined as sum of the free surfaces of the holes in the upstream perforated plate related to the entire cross-section area vertical to the supply direction of the feed gas flow to the mixing device of = 0.3. The downstream perforated plate is spaced from the flowing level of the ribbed tubes around 0.5-2 times of the diameter of the ribbed tubes to the last row of the ribbed tubes. A distance of the downstream perforated plate for entering the reaction mixture into the catalyst bed is 5-20 times of the diameter of the holes in the downstream perforated plate. An independent claim is included for a procedure for continuous oxide hydrogenation of a feed gas flow of saturated hydrocarbons.

公开(公告)号：AT499336T

公开(公告)日：2011-03-15

申请号：AT05849467

申请日：2005-12-07

Applicant: BASF SE

Inventor： CRONE SVEN ,  KLANNER CATHARINA ,  SCHINDLER GOETZ-PETER ,  DUDA MARK ,  BORGMEIER FRIEDER

IPC: C07C5/333 ,  C07C11/167

Abstract: A process for preparing butadiene, comprising nonoxidatively dehydrogenating n-butane from a stream (a) in a first dehydrogenation zone to obtain stream (b) comprising 1-butene and 2-butene; oxidatively dehydrogenating the 1-butene and 2-butene of (b) in the presence of an oxygenous gas in a second dehydrogenation zone to obtain stream (c) comprising n-butane, butadiene, hydrogen, carbon dioxide, and steam; compressing and cooling (c) to obtain stream (d2) comprising n-butane, butadiene, hydrogen, carbon dioxide, and steam; extractively distilling (d2) into stream (e1) comprising butadiene and stream (e2) comprising n-butane, hydrogen, carbon dioxide, and steam; compressing and cooling (e2) to obtain stream (f1) comprising n-butane and water and stream (f2) comprising n-butane, hydrogen, and carbon dioxide; cooling (f2) to obtain stream (g1) comprising n-butane and stream (g2) comprising carbon dioxide and hydrogen; phase separating water from (f1) to obtain stream (h1) comprising n-butane; and recycling (h1) into the first dehydrogenation zone.

公开(公告)号：AT466826T

公开(公告)日：2010-05-15

申请号：AT04804421

申请日：2004-12-30

Applicant: BASF SE

Inventor： JOHANN THORSTEN ,  SCHINDLER GOETZ-PETER ,  BRODHAGEN ANDREAS ,  CRONE SVEN ,  BENFER REGINA ,  HILL THOMAS ,  DUDA MARK

IPC: C07C5/333 ,  C07C5/48 ,  C07C11/167

Abstract: The disclosure relates to a process for preparing butadiene. The process involves nonoxidatively catalytically dehydrogenating butane to obtain a product gas stream containing butane, 1-butene, 2-butene, butadiene, hydrogen and secondary constituents. The 1-butene and 2-butene of the product gas stream is then oxidatively dehydrogenated to give a second gas stream containing butane,2-butene, butadiene, hydrogen, steam and secondary constituents. Next, the butane,2-butene and butadiene are separated from the second gas stream and the butane and 2-butene are then separated from the butadiene product. The butane and 2-butene are then recycled into the nonoxidative catalytic dehydrogenating zone.

公开(公告)号：MX2009000560A

公开(公告)日：2009-02-18

申请号：MX2009000560

申请日：2007-07-16

Applicant: BASF SE

Inventor： ROHDE WOLFGANG ,  CRONE SVEN ,  DEGEN GEORG ,  BOEHLING RALF ,  ALTENHOFF ANSGAR GEREON ,  BUERKLE JOCHEN ,  SCHINDLER GOETZ-GEORG ,  HOLTMAN THOMAS ,  SCHMITT MARKUS

IPC: C07C29/09 ,  C07C5/333 ,  C07C11/06 ,  C07C11/08 ,  C07C31/10 ,  C07C31/12 ,  C07C51/09 ,  C07C53/02 ,  C07C53/08 ,  C07C67/04 ,  C07C69/06 ,  C07C69/14

Abstract: Se proporciona un proceso para preparar alcanoles (I) seleccionados del grupo que consiste en isopropanol y 2-butanol a partir de los alcanos (II) correspondientes, seleccionados del grupo que consiste en propano y n-butano. El proceso consiste en los pasos de: (A) una corriente gaseosa de uso a que contiene el alcano (II); (B) la corriente gaseosa de uso a que contiene el alcano (II) se alimenta hacia una zona de deshidrogenación y el alcano (II) se somete a una deshidrogenación al alqueno (III) para obtener una corriente gaseosa de productos b que contiene el alqueno (III), alcano (II) no convertido, con o sin sustancias con punto de ebullición alto, vapor, hidrógeno y sustancias con punto de ebullición bajo; (C) la corriente gaseosa de productos b está al menos comprimida, y la corriente gaseosa de productos b se separa optativamente en una fase acuosa c1, una fase c2 que contiene el alqueno (III) y el alcano (II), con o sin sustancias de punto de ebullición alto, y una fase gaseosa c3 que contiene hidrógeno y sustancias de punto de ebullición bajo; (D) la corriente gaseosa de productos b o la fase c que contiene alqueno (III) y alcano (II) reacciona en una zona de esterificación con un ácido orgánico (IV) para obtener una mezcla de productos d que contienen el éster alquílico (V) correspondiente del ácido orgánico y el alcano (II) no convertido; (E) una corriente gaseosa el que contiene alcano (II) se separa de la mezcla de productos d y se recircula optativamente hacia la zona de deshidrogenación, y se obtiene una mezcla de productos e2 que contiene el éster alquílico; (F) la mezcla de productos e2 que contiene el éster alquílico reacciona en una zona de desesterificación con agua para obtener una mezcla de productos f que contiene el alcanol (I) y el ácido orgánico (IV); (G) el alcanol (I) y el ácido orgánico (IV) se separan de la mezcla de productos f, y como una opción, el ácido orgánico se recircula hacia la zona de esterificación.1.