公开(公告)号：WO2008095860A3

公开(公告)日：2008-12-24

申请号：PCT/EP2008051208

申请日：2008-01-31

Applicant: BASF SE ,  OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

IPC: C01B3/36

CPC classification number: F23C6/045 ,  B01J4/005 ,  C01B3/36 ,  C01B2203/0255 ,  C07C5/48 ,  F23C2900/06041 ,  F23L7/005 ,  Y02E20/344 ,  Y02P20/129 ,  C07C11/06 ,  C07C11/08

Abstract: The invention relates to a method for producing a gas flow comprising oxygen for the endothermic reaction of a starting flow, comprising one or more hydrocarbons, with a predefined concentration of oxygen and a predefined temperature, characterized in that a fluid fuel flow is burned with a primary air flow, with ?-values of the primary air flow to the fluid fuel flow ranging between 0.6 and 1.2, while preserving a combustion gas flow, and that a secondary air flow is mixed to the combustion gas flow, while preserving the gas flow comprising the oxygen for the endothermic reaction, wherein the volume flow and the temperature of the secondary air flow are used to adjust the predefined concentration of oxygen and the predefined temperature of the gas flow comprising the oxygen.

Abstract translation: 公开了一种用于为一个输出电流的吸热反应提供含氧气体流，其包含具有氧的预定浓度和预定温度，其特征在于，流体燃料流与在值的主空气流的一种或多种烃的方法？ 主气流至0.6〜1.2的流体燃料斯特罗姆被燃烧以产生燃烧气体流和二次空气流混合以含有给用于吸热反应的氧气流量的燃烧气体流，其中，在所述质量流量和二次空气流的温度 所述氧的预定浓度，以及所述含氧气体流的预定温度可以调节。

公开(公告)号：DE102006060509A1

公开(公告)日：2008-06-26

申请号：DE102006060509

申请日：2006-12-19

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

IPC: B01J8/02 ,  C07B35/04 ,  C07C5/333 ,  C07C11/06 ,  C07C11/08

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：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：DE102006060507A1

公开(公告)日：2008-06-26

申请号：DE102006060507

申请日：2006-12-19

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

IPC: B01J8/02

Abstract: A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid starting material stream, two/three rows arranged behind one another of tubes which have turbulence generators on the outside, a perforated plate upstream of the tubes and a perforated plate downstream of the tubes. A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid stream, two/three rows of tubes arranged behind one another and having turbulence generators on the outside, and constrict the flow cross section for the first fluid starting material stream to from 1/2 to 1/10, with the second fluid starting material stream being passed through the interiors of the tubes and injected via openings in the tubes into the first fluid starting material stream; a perforated plate upstream of the tubes; and a perforated plate downstream of the tubes. Independent claims are included for the following (1) mixing-in device for the reactor; and (2) static mixer for at least two fluid composed of the elements of the mixing-in device.

公开(公告)号：ZA200904965B

公开(公告)日：2010-09-29

申请号：ZA200904965

申请日：2009-07-16

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CRONE SVEN ,  CORR FRANZ

IPC: B01F20060101 ,  B01J20060101

Abstract: A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid starting material stream, two/three rows arranged behind one another of tubes which have turbulence generators on the outside, a perforated plate upstream of the tubes and a perforated plate downstream of the tubes. A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid stream, two/three rows of tubes arranged behind one another and having turbulence generators on the outside, and constrict the flow cross section for the first fluid starting material stream to from 1/2 to 1/10, with the second fluid starting material stream being passed through the interiors of the tubes and injected via openings in the tubes into the first fluid starting material stream; a perforated plate upstream of the tubes; and a perforated plate downstream of the tubes. Independent claims are included for the following (1) mixing-in device for the reactor; and (2) static mixer for at least two fluid composed of the elements of the mixing-in device.

公开(公告)号：BRPI0720412A2

公开(公告)日：2013-12-31

申请号：BRPI0720412

申请日：2007-12-14

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

IPC: B01F5/04 ,  B01J8/00 ,  B01J8/02 ,  B01J8/04

Abstract: A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid starting material stream, two/three rows arranged behind one another of tubes which have turbulence generators on the outside, a perforated plate upstream of the tubes and a perforated plate downstream of the tubes. A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid stream, two/three rows of tubes arranged behind one another and having turbulence generators on the outside, and constrict the flow cross section for the first fluid starting material stream to from 1/2 to 1/10, with the second fluid starting material stream being passed through the interiors of the tubes and injected via openings in the tubes into the first fluid starting material stream; a perforated plate upstream of the tubes; and a perforated plate downstream of the tubes. Independent claims are included for the following (1) mixing-in device for the reactor; and (2) static mixer for at least two fluid composed of the elements of the mixing-in device.

公开(公告)号：DE10232967B4

公开(公告)日：2011-12-01

申请号：DE10232967

申请日：2002-07-19

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CORR FRANZ

IPC: B01J8/06 ,  F04D29/08 ,  B01J19/00 ,  B01J19/24 ,  C07B33/00 ,  C07C27/14 ,  C07C45/35 ,  C07C47/127 ,  C07C47/22 ,  C07C51/25 ,  C07C57/04 ,  C07C57/05 ,  C07C59/153 ,  C07D307/32 ,  C07D307/60 ,  C07D307/89 ,  F04D7/06 ,  F04D11/00 ,  F04D29/04 ,  F04D29/047 ,  F28D7/00 ,  F28F27/02

Abstract: Reaktor (1) mit einem Bündel von Kontaktrohren (2), durch die ein Reaktionsgemisch und durch dessen die Kontaktrohre (2) umgebenden Raum ein Wärmetauschmittel (3) geleitet wird, mit Ringleitungen (4, 5) an beiden Reaktorenden mit Mantelöffnungen (6, 7) für die Zu- bzw. Abführung des Wärmetauschmittels (3) mittels einer oder mehrerer Pumpen (8), wobei das Wärmetauschmittel (3) der oberen Ringleitung (4) zugeführt und über die untere Ringleitung (5) von der (den) Pumpe(n) (8) mit vertikaler (vertikalen) Pumpenwelle(n) (9), die an ihrem oberen Ende gelagert und angetrieben wird (werden), angesaugt wird, dadurch gekennzeichnet, dass die Pumpe(n) (8) ein Diagonallaufrad (10) sowie einen Drosselspalt (11) in Längsrichtung der Pumpenwelle(n) (9), innerhalb des Wärmetauschmittels (3) auf der Druckseite der Pumpe(n) (8) zur Abdichtung und Lagerung der Pumpenwelle(n) (9) und Achsschubverminderung des Diagonallaufrads (10) aufweist (aufweisen).

公开(公告)号：SG153458A1

公开(公告)日：2009-07-29

申请号：SG200904205

申请日：2007-12-14

Applicant: BASF SE

Inventor： OLBERT GERHARD ,  CORR FRANZ ,  CRONE SVEN

Abstract: A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid starting material stream, two/three rows arranged behind one another of tubes which have turbulence generators on the outside, a perforated plate upstream of the tubes and a perforated plate downstream of the tubes. A reactor (1) for carrying out a reaction between two fluid starting materials (2, 3) over a catalyst bed (4) with premixing of the fluid starting materials before introduction into the catalyst bed within a delay time of less than 150 minutes comprises a mixing-in device (5) containing transversally arranged to the inflow direction of the first fluid stream, two/three rows of tubes arranged behind one another and having turbulence generators on the outside, and constrict the flow cross section for the first fluid starting material stream to from 1/2 to 1/10, with the second fluid starting material stream being passed through the interiors of the tubes and injected via openings in the tubes into the first fluid starting material stream; a perforated plate upstream of the tubes; and a perforated plate downstream of the tubes. Independent claims are included for the following (1) mixing-in device for the reactor; and (2) static mixer for at least two fluid composed of the elements of the mixing-in device.