32.
    发明专利
    未知

    公开(公告)号:DE102008042010A1

    公开(公告)日:2009-04-16

    申请号:DE102008042010

    申请日:2008-09-12

    Applicant: BASF SE

    Abstract: The procedure for continuous separation of target product (X) in the form of fine particle of crystallisate from a liquid phase (P) existing from the target product (X) and/or by the target product of different constituents, comprises indirectly operating a heat exchanger having primary and secondary areas, which are spatially separated with one another through a material divider that serves as an area for transmitting heat from the secondary area to the primary area by passing a stream at the liquid phase (P) in the secondary area of the heat exchanger. The procedure for continuous separation of target product (X) in the form of fine particle of crystallisate from a liquid phase (P) existing from the target product (X) and/or by the target product of different constituents, comprises indirectly operating a heat exchanger having primary and secondary areas, which are spatially separated with one another through a material divider that serves as an area for transmitting heat from the secondary area to the primary area by passing a stream at the liquid phase (P) in the secondary area of the heat exchanger during the primary area flows throughable simultaneously to a liquid cooling medium so that it forms fine particles of crystallisate of the target product in the secondary area under disposition of a liquid residual phase from the liquid phase (P). The total mole fraction of the liquid phase has the value of M b, p ges at the constituent (B i). The liquid residual phase (R) contains ingredients with a total mole fraction of M b, r (ges) greater than M b, p (ges) in comparison with the liquid phase (P). The content of residual phase in the target product is 70 wt.%. The cooling medium is suspended by fine particles of crystallisate of the target product in the liquid residual phase under receiving a suspension (S) having a crystallization grade (Y). The secondary area of the heat exchanger continuously takes the suspension with the temperature T s (aus). The suspension of fine particle crystallisate from the extracted suspension in load of discharge device is introduced with temperature (TS) to a mixing buffer container by a pump and the liquid phase is separated from the suspension contained in the discharge device. The temperature of the suspension in the buffer container is elevated from the way of secondary area in the buffer container and/or pipelines of the buffer container by external energy source at a value of T(pu) above of T s(aus) and/or the total mole fraction of the ingredients is increased in the liquid residual phase of the suspension in the buffer container through external additive in the ingredients at a value of M b, p u (ges) above of M b, r (ges). The T(pu)-T s(aus) is greater than or equal to 0.1 K. The increasing of M b, r ges at M b, r (ges) is greater than or equal to 0.1%. The content of the liquid residual phase at the target product is greater than or equal 90 wt.%. The crystallization grade (Y) is 0.20-0.40.

    Production of acrylic acid by partial gas phase oxidation, for use e.g. as monomer, includes extracting acrylic acid with organic solvent from acidic stream obtained in purification column

    公开(公告)号:DE102007004960A1

    公开(公告)日:2008-07-31

    申请号:DE102007004960

    申请日:2007-01-26

    Applicant: BASF SE

    Abstract: In production of acrylic acid (I) by partial gas phase oxidation, where the product gas mixture (containing (I), steam and by-products) is selectively condensed in a column and part of a withdrawn acidic water stream (containing (I)) is recycled to the column, (I) is extracted with an organic solvent from another part of the acidic water and (I) is thermally separated from the extract before recycling, purifying and/or taking up in alkali. In the production of acrylic acid (I) by partial gas phase oxidation of 3C precursor(s) (II) with oxygen over a solid catalyst at elevated temperature, the product gas mixture containing (I), steam and by-products (III) (optionally after (in)direct cooling) is passed upwards through a selective condensation column with separators. Water and (III) are withdrawn at a first side outlet above the introduction site; acidic water containing (I) and (III) is withdrawn at a second, higher side outlet; a residual gas containing lower-boiling (III) is withdrawn at the head; and a liquid containing (I) and higher boiling (III) is obtained at the sump. Part of the acidic water is recycled to the column (optionally after cooling) and the crude (I) is purified by further thermal treatment. The novel features are that (I) is extracted with an organic solvent (IV) from another part of the acidic water; (I) is thermally separated from the obtained solution of (I) in (IV); and the obtained (I) is recycled to the column, or is further purified and/or taken up in aqueous metal hydroxide solution.

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