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    3.
    发明专利
    未知

    公开(公告)号：BRPI0517615A

    公开(公告)日：2008-10-14

    申请号：BRPI0517615

    申请日：2005-11-11

    Applicant: BASF AG

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

    IPC: C07C5/333 ,  C07C11/167

    Abstract: Processes for producing butadiene from n-butane comprising: (a) providing a feed gas stream comprising n-butane; (b) non-oxidatively dehydrogenating the feed gas stream in the presence of a catalyst in a first dehydrogenation zone to form a first intermediate gas stream comprising n-butane, 1-butene, 2-butene, butadiene and hydrogen; (c) oxidatively dehydrogenating the first intermediate gas stream in the presence of an oxygenous gas having an oxygen content of at least 75% by volume in a second dehydrogenation zone to form a second intermediate gas stream comprising n-butane, butadiene, hydrogen, carbon dioxide and steam; (d) compressing and cooling the second intermediate gas to form a first condensate stream comprising water and a third intermediate gas stream comprising n-butane, butadiene, hydrogen, carbon dioxide and steam; (e) compressing and cooling the third intermediate gas to form a second condensate stream comprising n-butane, butadiene and water and a fourth intermediate gas stream comprising n-butane, butadiene, hydrogen and carbon dioxide; (1) cooling the fourth intermediate gas stream to form a third condensate stream comprising n-butane and butadiene, and an offgas stream comprising carbon dioxide and hydrogen; (g) removing water from the second condensate stream and combining the second condensate stream and third condensate stream to form a C 4 hydrocarbon stream comprising n-butane and butadiene; and (h) separating the C 4 hydrocarbon stream to form a recylce stream comprising n-butane and a product stream comprising butadiene; wherein at least a portion of the recycle stream is fed to the first dehydrogenation zone.

    Preparing dehydrogenated hydrocarbon comprises providing a gaseous reaction mixture stream containing hydrocarbon at an increased temperature through a catalyst bed system, and supplying a volume flow of e.g. molecular oxygen
    4.
    发明专利
    Preparing dehydrogenated hydrocarbon comprises providing a gaseous reaction mixture stream containing hydrocarbon at an increased temperature through a catalyst bed system, and supplying a volume flow of e.g. molecular oxygen 未知

    公开(公告)号：DE102006035718A1

    公开(公告)日：2008-01-31

    申请号：DE102006035718

    申请日：2006-07-28

    Applicant: BASF AG

    Inventor： DIETERLE MARTIN ,  KLANNER CATHARINA ,  SCHINDLER GOETZ-PETER ,  MUELLER-ENGEL KLAUS JOACHIM ,  SCHEIDEL JENS ,  ADAMI CHRISTOPH

    IPC: C07C5/333 ,  C07C11/00 ,  C07C11/02 ,  C07C57/05 ,  C07C57/07 ,  C07C67/08 ,  C07C69/54 ,  C08F20/10

    Abstract: Preparation of dehydrogenated hydrocarbon, comprises providing a gaseous reaction mixture stream containing the hydrocarbon at an increased temperature through a catalyst bed system present in a reaction zone; and optionally supplying a volume flow of molecular oxygen, molecular hydrogen, water vapor and/or another inert gas that act as auxiliary gases for the dehydrogenation reaction, to the gaseous reaction mixture stream between its entry at the start of the catalyst bed system and its exit from the end of the catalyst bed system. Procedure for the long-term operation of a continuously-operated and heterogeneously-catalyzed partial dehydrogenation process of a hydrocarbon to be dehydrogenated to form a dehydrogenated hydrocarbon, comprises providing a gaseous reaction mixture stream containing the hydrocarbon in an initial molar volume (KW), at an increased temperature through a catalyst bed system, which is present in a reaction zone (RZ) and consist of many catalyst bed sections that are arranged serially along the flow direction of the gaseous reaction mixture stream, and as a whole consists a molar volume (M) of a dehydrogenation catalyst; where: at the time of operation t is t 0, the passage of the gaseous reaction mixture stream through first, second and last third portion of (M) along the flow direction output, proportions of A, B and C mol.% of (KW) of the hydrocarbon to be dehydrogenated are respectively converted to form dehydrogenated hydrocarbon, under the condition that A is greater than B and B is greater than C and during the passage of the gaseous reaction mixture stream through the catalyst bed system, a total (G) i.e. A+B+C mol.% of (KW) of the hydrocarbon to be dehydrogenated that is contained in this reaction mixture stream is dehydrogenated to form dehydrogenated hydrocarbon, and optionally supplying a volume flow of molecular oxygen, molecular hydrogen, water vapor and/or another inert gas that act as auxiliary gases for the dehydrogenation reaction, to the gaseous reaction mixture stream between its entry at the start of the catalyst bed system and its exit from the end of the catalyst bed system, where deactivation of the catalyst bed system that advances with increasing operating time within an operation time interval of greater than t 0 and less than t r is counteracted by varying the temperature profile of the gaseous reaction mixture stream within the catalyst bed system and/or the volume flow of the optionally supplied auxiliary gases for the dehydrogenation reaction, where t r is the operating time point at which the dehydrogenation is interrupted and the catalyst bed system is at first recovered after the operating time point of t 0, thus the variation is carried out in such a manner that with increasing operating time point, the proportion A decreases, the proportion B undergoes a maximum and the proportion C increases.

    Preparation of acrolein/acrylic acid comprises supplying gas mixture stream A to zone A, supplying propane gas stream to obtain product gas mixture; dividing product stream A into two component streams; feeding a stream to zone B
    5.
    发明专利
    Preparation of acrolein/acrylic acid comprises supplying gas mixture stream A to zone A, supplying propane gas stream to obtain product gas mixture; dividing product stream A into two component streams; feeding a stream to zone B 未知

    公开(公告)号：DE102005049699A1

    公开(公告)日：2007-04-19

    申请号：DE102005049699

    申请日：2005-10-14

    Applicant: BASF AG

    Inventor： KLANNER CATHARINA ,  DIETERLE MARTIN ,  SCHINDLER GOETZ-PETER ,  CHENG TSUNG-CHIEH ,  MUELLER-ENGEL KLAUS JOACHIM

    IPC: C07C57/05 ,  B01J12/00 ,  C07C5/333 ,  C07C11/06 ,  C07C45/28 ,  C07C47/22

    Abstract: Preparation of acrolein/acrylic acid from propane comprises supplying reaction gas mixture input stream A to a reaction zone A; supplying dehydrogenated propane gas stream to obtain a product gas mixture; removing the product mixture stream A; dividing the product gas mixture stream A into component streams (I) and (II); feeding the component stream (II) in a second reaction zone B into an oxidative reactor, in which propylene in stream (II) is oxidized to form a product gas mixture B containing e.g. acrolein/acrylic acid as final product and separating the final product. Preparation of acrolein and/or acrylic acid from propane comprises supplying a reaction gas mixture input stream A (which is produced by merging at least four different gaseous initial streams 1, 2, 3 and 4) to the inlet of the first reaction zone A by at least a catalyst bed; optionally further supplying partially, heterogeneously catalyzed dehydrogenated propane gas stream to the mixture to obtain a product gas mixture containing propane and propylene; removing the obtained product gas mixture stream A from the first reaction zone A by discharge opening; dividing the product gas mixture stream A into two component streams (I) and (II) with identical composition, where the component stream (I) is fed back as gaseous initial stream 1 into the first reaction zone A in a first gas cycle operation and the component stream (II) is optionally led into the first separation zone A, to separate partial or large quantity of different propane and propylene components and to produce a residual product gas mixture stream A1 containing propane and propylene; feeding the component stream (II) or the product gas mixture in a second reaction zone B into at least an oxidative reactor, in which the propylene contained in the component stream (II) or in the product gas mixture stream A1 is subjected to selective heterogeneously catalyzed partial gaseous phase oxidation with molecular oxygen to form a product gas mixture B containing acrolein and/or acrylic acid as final product, optionally unconverted propane and propylene, and surplus molecular oxygen; removing the product gas mixture stream B from the reaction zone B; separating the final product, where the residual gas containing unconverted propane and propylene, and molecular oxygen is fed back as gaseous initial stream 2 in a second gas cycle operation into the reaction zone A (when the gaseous initial streams 2, 3 and 4 and optionally a gaseous stream different from the 1 are merged to a single propelled jet gaseous mixture stream); and subsequently operating the mixture with gaseous propelled jet mixture stream as propelled jet of a jet pump, which comprises a jet nozzle, a mixing path, a diffuser and a suction intake socket; where the direction of the propulsion of the propelled jet by the jet nozzle over a mixing path and the diffuser, points towards the inlet of the first reaction zone A and the suction effect of the suction intake socket, points towards the direction of the discharge opening of the first reaction zone A leading to the product gas mixture stream A and the component stream (I) is sucked through the negative pressure produced in the suction intake socket along with the splitting up of the product gas mixture A into the two component stream, and is transported with simultaneous mixing of propelled jet by the mixing path over the diffuser and the obtained reaction gas mixture input stream A is left into the inlet of the first reaction zone A; the gaseous initial streams 1, 2 and 3 is a propane, the gaseous initial stream 4 is a molecular hydrogen and the gaseous initial stream 3 is a fresh propane; the first gaseous initial stream 2 and 3 and optionally stream 1 and stream 4 are combined in an arbitrary sequence to a single gaseous mixture stream and stream 4 is added to the gaseous initial mixture stream under the formation of the gaseous propelled jet mixture stream.

    Continuous heterogeneously catalyzed partial dehydrogenation of hydrocarbon involves dehydrogenation through catalyst bed disposed in reaction chamber and with generation of product gas
    6.
    发明专利
    Continuous heterogeneously catalyzed partial dehydrogenation of hydrocarbon involves dehydrogenation through catalyst bed disposed in reaction chamber and with generation of product gas 未知

    公开(公告)号：DE102006029790A1

    公开(公告)日：2008-01-03

    申请号：DE102006029790

    申请日：2006-06-27

    Applicant: BASF AG

    Inventor： HECHLER CLAUS ,  RUPPEL WILHELM ,  SCHINDLER GOETZ-PETER ,  KLANNER CATHARINA ,  BASSLER HANS-JUERGEN ,  DIETERLE MARTIN ,  KLAPPERT KARL-HEINRICH ,  MUELLER-ENGEL KLAUS JOACHIM

    IPC: C07C5/333 ,  B01J19/02 ,  C07C7/09 ,  C07C7/12 ,  C07C11/00 ,  C07C45/34 ,  C07C47/22 ,  C07C57/05 ,  C07C57/07 ,  C08F20/06 ,  C08F20/20 ,  C22C38/40

    Abstract: Continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in the gas phase involves at least one catalyst bed disposed in the reaction chamber and with generation of a product gas comprising the at least one dehydrogenated hydrocarbon, unconverted hydrocarbon to be dehydrogenated and molecular hydrogen and/or steam, is dehydrogenated partially in an oxidative or non-oxidative manner to at least one dehydrogenated hydrocarbon, and at least one product gas stream is withdrawn continuously from the reaction chamber. Process for continuous heterogeneously catalyzed partial dehydrogenation of at least one hydrocarbon to be dehydrogenated in the gas phase involves a reaction chamber enclosed by a shell which is in contact with the reaction chamber and has at least one first orifice for feeding at least one starting gas stream into the reaction chamber and at least one second orifice for withdrawing at least one product gas stream from the reaction chamber, at least one starting gas stream comprising at least one hydrocarbon to be dehydrogenated is fed continuously in the reaction chamber. The at least one hydrocarbon to be dehydrogenated is conducted through at least one catalyst bed disposed in the reaction chamber and with generation of a product gas comprising the at least one dehydrogenated hydrocarbon, unconverted hydrocarbon to be dehydrogenated and molecular hydrogen and/or steam, is dehydrogenated partially in an oxidative or non-oxidative manner to at least one dehydrogenated hydrocarbon, and at least one product gas stream is withdrawn continuously from the reaction chamber. The shell is manufactured from a composite material which, on its side B in contact with the reaction chamber, consists of steel B comprising (wt.%): chromium (18-30), nickel (9-37), silicon (1-4), aluminum (>=0-4), nitrogen (>=0-0.3), carbon (>=0-0.15), manganese (>=0-4), phosphorus (>=0-0.05), sulfur (>=0-0.05), and at least one rare earth metal (>=0-0.1), and iron and impurities resulting from production. The steel B, on its side A facing away from the reaction chamber, is plated either directly or via an intermediate layer of copper, and/or nickel, onto steel A comprising (wt.%): chromium (15-20), nickel (6-18), silicon (>=0-0.8), aluminum (>=0-0.8), nitrogen (>=0-0.3), carbon (>=0-0.15), molybdenum (>=0-4), manganese (>=0-2), titanium (>=0-0.8), niobium (>=0-1.2), vanadium (>=0-0.9), boron (>=0-0.1), phosphorus (>=0-0.05), sulfur (>=0-0.05), iron and impurities resulting from production, or a composition comprising (wt.%) Cr (19-23), Ni (30-35), Co (>=0-1), Si (>=0-1), Al (0.15-0.7), C (>=0-0.12), Mn (>=0-2), Cu (>=0-0.75), Ti (0.15-0.7), Nb (>=0-0.1), P (>=0-0.05), S (>=0-0.05) and iron and impurities resulting from production. An independent claim is included for a shell encloses an interior and has at least one first orifice for feeding at least one gas stream into the interior and at least one second orifice for withdrawing a gas stream fed to the interior beforehand via the at least one first orifice O1 from the interior. The shell is manufactured from a composite material which, on its side B in contact with the reaction chamber, consists of steel B on its side A facing away from the reaction chamber is plated either directly or via an intermediate layer of copper and/or nickel onto steel A.

    7.
    发明专利
    未知

    公开(公告)号：DE102004059356A1

    公开(公告)日：2006-06-14

    申请号：DE102004059356

    申请日：2004-12-09

    Applicant: BASF AG

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

    IPC: C07C5/327 ,  C07C7/00 ,  C07C11/16

    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.

    8.
    发明专利
    未知

    公开(公告)号：BRPI0606630A2

    公开(公告)日：2010-01-19

    申请号：BRPI0606630

    申请日：2006-01-16

    Applicant: BASF AG

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

    IPC: C07C5/333 ,  C07C11/167

    Abstract: A process for preparing butadiene, comprising A) providing a stream (a) comprising n-butane; B) feeding stream (a) comprising into at least one first dehydrogenation zone and nonoxidatively catalytically dehydrogenating n-butane to obtain a stream (b) comprising n-butane, 1-butene, 2-butene, butadiene, hydrogen and low-boiling secondary constituents; C) feeding stream (b) and an oxygenous gas into at least one second dehydrogenation zone and oxidatively dehydrogenating n-butane, 1-butene and 2-butene to obtain a stream (c) comprising n-butane, 2-butene, butadiene, low-boiling secondary constituents, carbon oxides and steam, wherein stream (c) has a higher content of butadiene than stream (b); D) removing the low-boiling secondary constituents and steam to obtain a stream (d) substantially consisting of n-butane, 2-butene and butadiene; E) separating stream (d) into a stream (e1) consisting substantially of n-butane and 2-butene and a stream (e2) consisting substantially of butadiene by extractive distillation; F) recycling stream (e1) into the first dehydrogenation zone.

    9.
    发明专利
    未知

    公开(公告)号：BRPI0518872A2

    公开(公告)日：2008-12-16

    申请号：BRPI0518872

    申请日：2005-12-07

    Applicant: BASF AG

    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.

    Preparation of acrolein/acrylic acid comprises supplying gas mixture stream A to zone A, supplying propane gas stream to obtain product gas mixture; dividing product stream A into two component streams; feeding a stream to zone B
    10.
    发明专利
    Preparation of acrolein/acrylic acid comprises supplying gas mixture stream A to zone A, supplying propane gas stream to obtain product gas mixture; dividing product stream A into two component streams; feeding a stream to zone B 未知

    公开(公告)号：DE102005051401A1

    公开(公告)日：2007-04-26

    申请号：DE102005051401

    申请日：2005-10-25

    Applicant: BASF AG

    Inventor： KLANNER CATHARINA ,  DIETERLE MARTIN ,  SCHINDLER GOETZ-PETER ,  CHENG TSUNG-CHIEH ,  MUELLER-ENGEL KLAUS JOACHIM

    IPC: C07C57/05 ,  B01J8/02 ,  B01J19/24 ,  C07C5/333 ,  C07C45/28 ,  C07C47/22 ,  C07C57/055

    Abstract: Preparation of acrolein/acrylic acid from propane comprises supplying reaction gas mixture input stream A to a reaction zone A; supplying dehydrogenated propane gas stream to obtain a product gas mixture; removing the product mixture stream A; dividing the product gas mixture stream A into component streams (I) and (II); feeding the component stream (II) in a second reaction zone B into an oxidative reactor, in which propylene in stream (II) is oxidized to form a product gas mixture B containing e.g. acrolein/acrylic acid as final product and separating the final product. Preparation of acrolein and/or acrylic acid from propane comprises supplying a reaction gas mixture input stream A (which is produced by merging at least four different gaseous initial streams 1, 2, 3 and 4) to the inlet of the first reaction zone A by at least a catalyst bed; optionally further supplying partially, heterogeneously catalyzed dehydrogenated propane gas stream to the mixture to obtain a product gas mixture containing propane and propylene; removing the obtained product gas mixture stream A from the first reaction zone A by discharge opening; dividing the product gas mixture stream A into two component streams (I) and (II) with identical composition, where the component stream (I) is fed back as gaseous initial stream 1 into the first reaction zone A in a first gas cycle operation and the component stream (II) is optionally led into the first separation zone A, to separate partial or large quantity of different propane and propylene components and to produce a residual product gas mixture stream A1 containing propane and propylene; feeding the component stream (II) or the product gas mixture in a second reaction zone B into at least an oxidative reactor, in which the propylene contained in the component stream (II) or in the product gas mixture stream A1 is subjected to selective heterogeneously catalyzed partial gaseous phase oxidation with molecular oxygen to form a product gas mixture B containing acrolein and/or acrylic acid as final product, optionally unconverted propane and propylene, and surplus molecular oxygen; removing the product gas mixture stream B from the reaction zone B; separating the final product, where the residual gas containing unconverted propane and propylene, and molecular oxygen is fed back as gaseous initial stream 2 in a second gas cycle operation into the reaction zone A (when the gaseous initial streams 2, 3 and 4 and optionally a gaseous stream different from the 1 are merged to a single propelled jet gaseous mixture stream); and subsequently operating the mixture with gaseous propelled jet mixture stream as propelled jet of a jet pump, which comprises a jet nozzle, a mixing path, a diffuser and a suction intake socket; where the direction of the propulsion of the propelled jet by the jet nozzle over a mixing path and the diffuser, points towards the inlet of the first reaction zone A and the suction effect of the suction intake socket, points towards the direction of the discharge opening of the first reaction zone A leading to the product gas mixture stream A and the component stream (I) is sucked through the negative pressure produced in the suction intake socket along with the splitting up of the product gas mixture A into the two component stream, and is transported with simultaneous mixing of propelled jet by the mixing path over the diffuser and the obtained reaction gas mixture input stream A is left into the inlet of the first reaction zone A; the gaseous initial streams 1, 2 and 3 is a propane, the gaseous initial stream 4 is a molecular hydrogen and the gaseous initial stream 3 is a fresh propane; the first gaseous initial stream 2 and 3 and optionally stream 1 and stream 4 are combined in an arbitrary sequence to a single gaseous mixture stream and stream 4 is added to the gaseous initial mixture stream under the formation of the gaseous propelled jet mixture stream.

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