公开(公告)号：DE102004031207A1

公开(公告)日：2006-01-19

申请号：DE102004031207

申请日：2004-06-28

Applicant: BASF AG

Inventor： BECKMANN STEFAN ,  WELCH DARRYL

IPC: B01D15/08 ,  C07C67/08 ,  C07C67/56 ,  C07C69/54

Abstract: Preparation of (meth)acrylic acid ester (I), comprises: preparing a reaction mixture (II) by catalytic gas phase partial oxidation, absorbing (II) and desorbing the loaded absorbent, subsequent rectificative purifying to obtain raw (meth)acrylic acid (III) and esterifying (III) with an alcohol (where water is not reversed into the rectification unit). Preparation of (meth)acrylic acid ester (I) comprises: preparing a reaction mixture (II) by catalytic gas phase partial oxidation of C3- or C4- precursors, absorbing (II) in an absorption apparatus with an absorbent, desorbing the loaded absorbent in a desorption apparatus by treating with a stripping gas, subsequent rectificative purifying of the absorbent to obtain raw (meth)acrylic acid (III) (where at least one absorption apparatus is operated with an absorbent quantity of 15-20 kg/m3> of (II); the temperature of the inlet to the desorption apparatus amounts to 120-140[deg]C and the amount of stripping gas in the desorption apparatus is more than 4 m3>/m3> of (II)) and esterifying (III) with an alcohol, where in the esterification step, water is not reversed into the rectification unit III.

公开(公告)号：DE10251138A1

公开(公告)日：2003-11-27

申请号：DE10251138

申请日：2002-10-31

Applicant: BASF AG

Inventor： DIEHL VOLKER ,  BECKMANN STEFAN ,  WELCH DARRYL

IPC: C07C51/44 ,  C07C51/47 ,  C07C67/08 ,  C07C67/54 ,  C07C69/54 ,  C07C57/05 ,  C07C67/03

Abstract: A process for the production of (meth)acrylic acid comprises use of 15-20 kg of absorption agent per m3 of reaction gas mixture; an inlet temperature of the desorption apparatus of 120-140 degrees C; and a quantity of stripping gas greater than 4 m3 per m3 of reaction gas mixture. A process for the production of (meth)acrylic acid comprises: (a) preparation of a reaction gas mixture by catalytic gas phase partial oxidation of suitable 3-4C precursors; (b) absorption of the reaction mixture from (A) in at least one absorption apparatus with an absorption agent, desorption of the absorption agent in at least one desorption apparatus by treatment with a stripping gas and; (c) subsequent distillation of the absorption agent to yield crude (meth)acrylic acid whereby the absorption apparatus comprises 15-20 kg of absorption agent per m3 of reaction gas mixture; the inlet temperature of the desorption apparatus is 120-140 degrees C; and the quantity of stripping gas is greater than 4 m3 per m3 of reaction gas mixture.