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    СПОСОБ СНИЖЕНИЯ ТЕМПЕРАТУРЫ ГОРЯЧЕЙ ТОЧКИ НЕПОДВИЖНОГО СЛОЯ КАТАЛИЗАТОРА В ПРОЦЕССЕ ПОЛУЧЕНИЯ АКРОЛЕИНА ИЛИ АКРИЛОВОЙ КИСЛОТЫ ИЛИ ИХ СМЕСИ ГЕТЕРОГЕННО КАТАЛИЗИРУЕМЫМ ЧАСТИЧНЫМ ОКИСЛЕНИЕМ В ГАЗОВОЙ ФАЗЕ
    41.
    发明专利
    СПОСОБ СНИЖЕНИЯ ТЕМПЕРАТУРЫ ГОРЯЧЕЙ ТОЧКИ НЕПОДВИЖНОГО СЛОЯ КАТАЛИЗАТОРА В ПРОЦЕССЕ ПОЛУЧЕНИЯ АКРОЛЕИНА ИЛИ АКРИЛОВОЙ КИСЛОТЫ ИЛИ ИХ СМЕСИ ГЕТЕРОГЕННО КАТАЛИЗИРУЕМЫМ ЧАСТИЧНЫМ ОКИСЛЕНИЕМ В ГАЗОВОЙ ФАЗЕ 未知

    公开(公告)号：RU2416595C2

    公开(公告)日：2011-04-20

    申请号：RU2007103613

    申请日：2005-05-04

    Applicant: BASF AG

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

    IPC: B01J8/04 ,  C07C45/33 ,  C07C45/35 ,  C07C47/22 ,  C07C51/16 ,  C07C51/215 ,  C07C51/235 ,  C07C51/25 ,  C07C57/05 ,  C07C57/055

    Abstract: Изобретениеотноситсяк усовершенствованномуспособуснижениятемпературыгорячейточкинеподвижногослоякатализаторав процессеполученияакролеинаилиакриловойкислотыилиихсмесигетерогеннокатализируемымчастичнымокислениемв газовойфазепропена, прикоторомисходнуюсмесь 2 реакционногогаза, содержащуюпропилени молекулярныйкислород, атакжемолекулярныйазоти пропанв качествеинертныхгазов-разбавителей, вкотороймолярноеотношениемолекулярногокислородак пропилену O2:С3Н6≥1, приповышеннойтемпературепропускаютчерезнеподвижныйслойкатализатора, активнаямассакоторогопредставляетсобой, поменьшеймере, одинполиметаллическийоксид, содержащийэлементыМо, Fe и Bi, вкоторомисходнаясмесь 2 реакционногогаза, впересчетенаобщийобъем, содержитот 7 до 9 об.% пропилена, от 9,8 до 15,5 об.% молекулярногокислорода, от 10,5 до 15,5 об.% пропанаи от 40 до 60 об.% молекулярногоазота, приусловии, чтомолярноеотношение V1 содержащегосяв исходнойсмеси 2 реакционногогазапропанак содержащемусяв исходнойсмеси 2 реакционногогазапропиленусоставляетот 1,5 до 2,2, молярноеотношение V2 содержащегосяв исходнойсмеси 2 реакционногогазамолекулярногоазотак содержащемусяв исходнойсмеси 2 реакционногогазамолекулярномукислородусоставляетот 3,5 до 4,5, амолярноеотношение V3 содержащегосяв исходнойсмеси 2 реакционногогазамолекулярногокислородак содержащемусяв исходнойсмеси 2 реакционногогазапропиленусоставляетот 1,4 до 2,14. 26 з.п. ф-лы, 1 ил., 3 табл.

    43.
    发明专利
    未知

    公开(公告)号：BRPI0607493A2

    公开(公告)日：2010-04-06

    申请号：BRPI0607493

    申请日：2006-03-01

    Applicant: BASF AG

    Inventor： HEILEK JOERG ,  MUELLER-ENGEL KLAUS JOACHIM ,  DIETERLE MARTIN ,  ADAMI CHRISTOPH

    IPC: C07C51/43 ,  C07C57/04

    Abstract: Disclosed is a method for eliminating methacrylic acid from a liquid phase (P) containing acrylic acid as a main component and target product and methacrylic acid as a secondary component. According to said method, the methacrylic acid is eliminated using crystallization, the acrylic acid accumulating in the formed crystallized product and the methacrylic acid accumulating in the remaining mother liquor.

    Heterogeneously-catalyzed partial direct oxidation of n-propane to acrylic acid comprises conducting initial reaction gas mixture comprising n-propane and molecular oxygen through a fixed bed catalyst and separating the acrylic acid
    47.
    发明专利
    Heterogeneously-catalyzed partial direct oxidation of n-propane to acrylic acid comprises conducting initial reaction gas mixture comprising n-propane and molecular oxygen through a fixed bed catalyst and separating the acrylic acid 未知

    公开(公告)号：DE102007029053A1

    公开(公告)日：2008-01-03

    申请号：DE102007029053

    申请日：2007-06-21

    Applicant: BASF AG

    Inventor： DIETERLE MARTIN ,  HEILEK JOERG ,  MUELLER-ENGEL KLAUS JOACHIM

    IPC: C07C57/05 ,  C07C57/07

    Abstract: Heterogeneously-catalyzed partial direct oxidation of n-propane to acrylic acid, comprises: conducting an initial mixture of reaction gases, which contain n-propane, molecular oxygen and at least an inert diluent gas, at elevated temperature through a fixed bed catalyst; subsequently transferring the obtained product gas containing acrylic acid into a first separation zone, in which the product gas is transferred into the liquid phase; separating the acrylic acid from the liquid phase in a second separation zone by at least a thermal separation procedure. Heterogeneously-catalyzed partial direct oxidation of n-propane to acrylic acid, comprises: conducting an initial mixture of reaction gases, which contain n-propane, molecular oxygen and at least an inert diluent gas, at elevated temperature through a fixed bed catalyst having a catalyst in a solid physical state, where the conversion of n-propane in the case of a single passage of the reaction gases through the catalyst bed amounts to >=10 mol.% and the selectivity of the acrylic acid formation, relative to the converted n-propane, amounts to >=40 mol.%; subsequently transferring the obtained product gas containing acrylic acid into a first separation zone, in which the product gas is transferred into the liquid phase; separating the remaining gases that contain n-propane and is depleted of acrylic acid, from the first separation zone; refluxing at least a partial quantity of the n-propane contained in the remaining product in the form of a gas to the reaction step; separating the acrylic acid from the liquid phase in a second separation zone by at least a thermal separation procedure. The initial mixture of reaction gases contains 2-50 vol.% of n-propane, 0.1-60 vol.% of carbon dioxide, 1-50 vol.% oxygen and 1-50 vol.% of water, related to its total volume, and up to 1 mol.% of cyclo-propane, related to the molar volume of n-propane contained in the initial mixture of reaction gases, The thermal separation process in the second separation zone comprises the separation of the acrylic acid by means of at least a crystallization step.

    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
    48.
    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：DE102005052917A1

    公开(公告)日：2007-10-11

    申请号：DE102005052917

    申请日：2005-11-03

    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 ,  C07C11/06 ,  C07C45/28 ,  C07C47/22 ,  C07C57/07

    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.

    Preparation of acrolein and/or acrylic acid useful for e.g. preparing polymers involves dehydrogenating propane to hydrogen and product gas comprising propylene; and oxidizing molecular hydrogen to steam and product gas to target products
    49.
    发明专利
    Preparation of acrolein and/or acrylic acid useful for e.g. preparing polymers involves dehydrogenating propane to hydrogen and product gas comprising propylene; and oxidizing molecular hydrogen to steam and product gas to target products 未知

    公开(公告)号：DE102005057197A1

    公开(公告)日：2007-06-06

    申请号：DE102005057197

    申请日：2005-11-29

    Applicant: BASF AG

    Inventor： MACHHAMMER OTTO ,  MUELLER-ENGEL KLAUS JOACHIM ,  DIETERLE MARTIN

    IPC: C07C47/22 ,  C07C45/35 ,  C07C57/05

    Abstract: Preparation of acrolein and/or acrylic acid (target product) involves: in reaction zone (A): partially dehydrogenating propane catalytically from a mixture of fresh propane and recycled mixture forming molecular hydrogen and propylene; oxidizing molecular hydrogen to steam and forming product gas (A); in reaction zone (B): partially oxidizing product gas (A) to product gas (B) comprising target product; in separation zones: removing target product from product gas (B), scrubbing of carbon dioxide present in the residual gas (I); and recycling residual gas (I) into reaction zone (A). Preparing acrolein and/or acrylic acid (target product) from propane involves: (i) in reaction zone (A): feeding gaseous streams of fresh propane, and recycled mixture to a first reaction zone (A) to form a reaction gas (A), passing the reaction gas A through at least one catalyst bed in which partial heterogeneously catalyzed dehydrogenation of the propane forms molecular hydrogen and propylene; oxidizing molecular hydrogen by molecular oxygen to steam; and feeding the resulting product gas (A) comprising molecular hydrogen, steam, propylene and propane is withdrawn from reaction zone (A) to reaction zone (B); (ii) in reaction zone (B), the product gas A from reaction zone A, with feeding of molecular oxygen, forming a reaction gas (B) comprising molecular hydrogen, steam, propane, propylene and molecular oxygen, and the propylene is subjected to a heterogeneously catalyzed partial gas phase oxidation to give a product gas (B) comprising target product, unconverted propane, molecular hydrogen, steam, carbon dioxide as a by-product, and also other secondary components having lower and higher boiling points than water; (iii) in a first separation zone: removing target product, water and secondary components having a higher boiling point than water present from the product gas (B) to leave a residual gas (I) comprising unconverted propane, carbon dioxide, molecular hydrogen, the secondary components and any unconverted propylene and any unconverted molecular oxygen; (iv) in second separation zone: as an aftertreatment measure (1), scrubbing out carbon dioxide present in residual gas (I) and condensing out water present if any; as an aftertreatment measure (2), discharging a remaining portion of residual gas (I); as aftertreatment treatment measure (3), removing molecular hydrogen by a separating membrane in a third separation zone (III); and as an aftertreatment measure (4), chemically reducing any molecular oxygen present in residual gas (I), where the sequence of use of aftertreatment measures 1 - 4 is as desired; and (v): recycling aftertreated residual gas (I) which comprises unconverted propane into reaction zone (A) as at least one of the two feed streams comprising propane. The amount of molecular hydrogen (M), which is at least 5 - 95 mol % of the total amount of molecular hydrogen produced in reaction zone (A) and that fed to reaction zone (A), is oxidized to steam in reaction zone (A).

    Preparing final products by partial oxidation of propylene, useful as intermediate for polymer, comprises subjecting propane to dehydrogenation, separating and subjecting the gas mixture in heterogeneous catalyzed gasphase-partial oxidation
    50.
    发明专利
    Preparing final products by partial oxidation of propylene, useful as intermediate for polymer, comprises subjecting propane to dehydrogenation, separating and subjecting the gas mixture in heterogeneous catalyzed gasphase-partial oxidation 未知

    公开(公告)号：DE102005022798A1

    公开(公告)日：2006-11-16

    申请号：DE102005022798

    申请日：2005-05-12

    Applicant: BASF AG

    Inventor： DIEFENBACHER ARMIN ,  HECHLER CLAUS ,  ADAMI CHRISTOPH ,  DIETERLE MARTIN

    IPC: C07C57/055 ,  B01J23/84 ,  C07C5/333 ,  C07C45/35 ,  C07C45/78 ,  C07C47/22 ,  C07C57/07 ,  C07C209/60 ,  C07C209/82 ,  C08F20/06

    Abstract: Preparation of at least one final product by partial oxidation and/or ammoxidation of propylene, comprises subjecting a purified propane to dehydrogenation; separating optionally the gas mixture containing propane and propylene, and simultaneously producing a propane and propylene containing gas mixture (II); subjecting the gas mixtures in heterogeneous catalyzed gasphase-partial oxidation, where a gas mixture (III) containing at least one final product is obtained; separating the gas mixture (III) and leading back at least propane in the remainder gas in the first reaction step. Preparation of at least one final product by partial oxidation and/or ammoxidation of propylene, comprises subjecting a propane, which is first purified in a first reaction step in the presence and/or absence of oxygen, to dehydrogenation comprising homogeneous dehydrogenation, heterogeneously catalyzed dehydration, homogeneous oxide-hydrogenation and heterogeneously catalyzed oxide-hydrogenation, where the non-reacted propane and formed propylene containing gas mixture (I) is obtained; separating optionally the total quantity or partial quantity of the gas mixture containing propane and propylene of different components and/or changing into other compounds, and simultaneously producing a propane and propylene containing gas mixture (II); subjecting the gas mixture (I) or (II), or a gas mixture, which is a mixture of formed gas mixture (II) and remained gas mixture (I) in heterogeneous catalyzed gasphase-partialoxidation and/or partial gasphase-ammoxidation of the gas mixture (I) and/or (II), where a gas mixture (III) containing at least one final product is obtained; and separating the gas mixture (III) and leading back at least propane in the remainder gas in the first reaction step, where the propane is pre-purified from raw propane, which contains >=90 wt.% of propane, =99 wt.% of propane and propylene, >=100 wt.% of 2C-hydrocarbon and >=100 wt.% of 4C-hydrocarbon, with the standard, that the raw propane leads to rectification column and takes place over the supply place of the purified propane, where the concentration of 2C-hydrocarbon of propane contained in the purified propane amounts to not more than 80 wt.% based on the content of raw propane and the concentration of 4C-hydrocarbon of propane contained in the purified propane amounts to a maximum of 50% based on the content of the raw propane.

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