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    PROCEDIMIENTO PARA ELIMINAR MERCAPTANOS DE CORRIENTES DE FLUIDOS QUE LOS CONTIENEN
    11.
    发明专利
    PROCEDIMIENTO PARA ELIMINAR MERCAPTANOS DE CORRIENTES DE FLUIDOS QUE LOS CONTIENEN 未知

    公开(公告)号：PE06042001A1

    公开(公告)日：2001-05-28

    申请号：PE0006882000

    申请日：2000-07-10

    Applicant: BASF AG

    Inventor： HUGO RANDOLF ,  WAGNER RUPERT ,  HOLST THOMAS S ,  GROSMANN CHRISTOPH

    IPC: B01D53/14 ,  C10L3/10

    CPC classification number: B01D53/1462 ,  B01D53/1487 ,  B01D53/1493 ,  Y02C10/06

    Abstract: DONDE DICHO PROCEDIMIENTO COMPRENDE: i) PONER EN CONTACTO LA CORRIENTE DE FLUIDOS EN UNA ZONA DE ABSORCION O EXTRACCION CON UN LIQUIDO DE LAVADO, EL CUAL CONTIENE: a) POR LO MENOS DE 10% A 70% EN PESO DE UNA ALCANOLAMINA ALIFATICA C2-C12, TAL COMO TRIETANOLAMINA O METILDIETANOLAMINA; b) COMO MAXIMO 5% EN PESO DE UN SOLVENTE FISICO PARA MERCAPTANOS; Y, c) DE 0% A 20% EN PESO DE UNA AMINA PRIMARIA O SECUNDARIA COMO ACTIVADOR, TAL COMO ALCANOLAMINA PRIMARIA O SECUNDARIA O UN N-HETEROCICLO DE 5 o 6 MIEMBROS SATURADO; ALIMENTANDO SUFICIENTE LIQUIDO DE LAVADO A DICHA ZONA, PARA QUE POR LO MENOS CO2 Y H2S SEAN ELIMINADOS SUSTANCIALMENTE EN FORMA COMPLETA DE LA CORRIENTE DE FLUIDOS; Y, b) SEPARAR LA CORRIENTE DE FLUIDOS PURIFICADA Y EL LIQUIDO DE LAVADO CARGADO, Y RETIRARLOS DE DICHA ZONA

    12.
    发明专利
    未知

    公开(公告)号：DE19947845A1

    公开(公告)日：2001-04-12

    申请号：DE19947845

    申请日：1999-10-05

    Applicant: BASF AG

    Inventor： WAGNER RUPERT ,  HUGO RANDOLF ,  HOLST TOM

    IPC: B01D53/14 ,  C10K1/14 ,  C10L3/10 ,  C07C7/11 ,  C07C7/10 ,  B01D11/04 ,  B01D53/48

    Abstract: The invention relates to a method for removing COS from a stream of hydrocarbon fluid containing COS, in particular, from a stream of gas, such as for example, natural gas, synthesis gas from heavy oil or heavy residues or refinery gas, or from liquid or liquefied hydrocarbons, such as for example, LPG (Liquefied Petroleum Gas) or NGL (Natural Gas Liquids) and to a wash liquid for use in methods of this type. The stream of fluid is brought into direct contact with the inventive wash fluid in an absorption or extraction zone. Said wash fluid consists of an aqueous amine solution which contains 1.5 to 5 moles/l of an aliphatic alkanolamine having between 2 and 12 C atoms and 0.4 to 1.7 moles/l of a primary or secondary amine as the activator. Substantially all of the COS is removed from the stream of fluid using the inventive amine wash. The stream of fluid which has been substantially cleaned of COS and the wash fluid which is loaded with COS are subsequently separated from one another and both fluids are fed out of the absorption or extraction zone. The wash fluid can subsequently be regenerated in the known manner and can be fed back to the absorption or extraction zone.

    14.
    发明专利
    未知

    公开(公告)号：DE19532051A1

    公开(公告)日：1997-03-06

    申请号：DE19532051

    申请日：1995-08-31

    Applicant: BASF AG

    Inventor： HERMELING DIETER DR ,  HUGO RANDOLF ,  SIEGEL HARDO DR

    IPC: C07F9/02 ,  C07F9/53

    Abstract: A process for purifying tert. phosphine oxides of formula (R )(R )(R )P = O (I) in which R , R and R = 1-12 C alkyl, 5-8 FC cycloalkyl, aryl, 7-20 C aralkyl or 7-20 C alkylaryl, comprises reacting the (I) or a (I)-contg. mixt., opt. in an inert solvent, with an (in)organic acid at 0-150 degrees C and subsequently reacting the resulting salt with water or an (in)organic base. Pref. reaction with the acid is pref. carried out in an inert solvent such as aromatic hydrocarbons, aliphatic hydrocarbons, cycloaliphatic hydrocarbons or aromatic nitriles. Suitable acids are eg mineral acids such as HCl, HClO4, H2SO4 or H3PO4, Lewis acids such as BF3 or AlCl3, or organic acids such as acetic acid, formic acid or oxalic acid. The ratio acid to impure (I) is pref. 0.3 : 1 to 20 : 1, esp. 0.7 : 1 to 2 : 1. After crystallisation, the salt is recovered eg by filtration or centrifuging. The free (I) is liberated by treating the salt eg with an (in)organic base, esp. an aq. soln. of a base such as NaOH, KOH, Na2CO3, NH3, triethylamine, etc. The (I) is recovered e.g. by extraction with an inert solvent in the usual way.

    15.
    发明专利
    未知

    公开(公告)号：DE502004005974D1

    公开(公告)日：2008-03-06

    申请号：DE502004005974

    申请日：2004-09-09

    Applicant: BASF AG

    Inventor： HUGO RANDOLF ,  WENZ KIRSTEN ,  WAMBSGANSS ROLF ,  JOURDAN SABINE ,  PREISS THOMAS

    IPC: C07C209/48 ,  C07C211/27

    Abstract: A process for preparing xylylenediamine by continuously hydrogenating liquid phthalonitrile over a heterogeneous catalyst in the presence of liquid ammonia in a reactor, which comprises mixing a stream of a phthalonitrile melt in liquid form by means of a mixer unit with a stream of liquid ammonia and conducting the liquid mixture into the hydrogenation reactor.

    Production of xylylenediamine by continuous hydrogenation of liquid, comprises mixing device phthalodinitrile as melt/in solid form that is mixed with stream of liquid ammonia and removing additional stream as partial stream
    18.
    发明专利
    Production of xylylenediamine by continuous hydrogenation of liquid, comprises mixing device phthalodinitrile as melt/in solid form that is mixed with stream of liquid ammonia and removing additional stream as partial stream 未知

    公开(公告)号：DE102005036222A1

    公开(公告)日：2007-02-08

    申请号：DE102005036222

    申请日：2005-08-02

    Applicant: BASF AG

    Inventor： HUGO RANDOLF ,  WENZ KIRSTEN ,  HUBER SABINE

    IPC: C07C209/48 ,  C07C209/84 ,  C07C209/86 ,  C07C211/27

    Abstract: The production of xylylene diamine by continuous hydrogenation of liquid, includes mixing device phthalodinitrile as melt/in solid form that is mixed with stream of liquid ammonia and removing additional stream as partial stream from the stream rotating around hydrogenation reactor or mixed with the streams. The mixing device is heated at 1-60[deg]C above the melting point of the phthalodinitrile. The mixture of streams is injected into the device. The liquid mixture of ammonia, phthalodinitrile and xylylene diamine is led into the stream rotating around the hydrogenation reactor. The production of xylylene diamine by continuous hydrogenation of liquid, includes mixing device phthalodinitrile as melt/in solid form that is mixed with stream of liquid ammonia and removing additional stream as partial stream from the stream rotating around hydrogenation reactor or mixed with the streams. The mixing device is heated at 1-60[deg]C above the melting point of the phthalodinitrile. The mixture of streams is injected into the device. The liquid mixture of ammonia, phthalodinitrile and xylylene diamine is led into the stream rotating around the hydrogenation reactor. The rotating stream is composed of larger than 93 wt% of liquid ammonia and xylylene diamine. The phthalodinitrile conversion in the hydrogenation reactor amount is larger than 99.5%. The mixture led into the hydrogenation reactor contains no solvent for phthalodinitrile. The stream rotating around the hydrogenation reactor contains liquid ammonia within the range of 25-90 wt%. A part of a liquid reactor discharge is led back continuously to the reactor entrance as rotating stream, constitutes 20-95 wt.% of the entire liquid reactor discharge. The weight ratio of the fresh phthalodinitrile inlet stream plus ammonia inlet stream to the stream rotating around the hydrogenation reactor lies between 0.05-5. The weight ratio of the feed back partial stream from the reactor discharge to the sum of the fresh phthalodinitrile inlet stream and ammonia inlet stream lies within the range of 2:1-10:1. The hydrogenation is accomplished at 40-150[deg] C, an absolute pressure of 100-300 bar and a manganese-doped complete cobalt catalyst. The catalyst is arranged in a tubular reactor or a bundle tube reactor as fixed bed. The hydrogenation reactor is adiabatically operated in trickle bed. The stream rotating around the hydrogenation reactor in which heat is extracted from a radiator. The hydrogenation reactor is used as a hydrogenation reactor cascade. The purification of the xylylenediamine takes place through distillation of ammonia in which light by-products collected at the top and heavy products collected at the bottom. The xylylenediamine is extracted after the distillation for further purification an organic solvent is added.

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