Detail of "5931-89-5"

Reference

Catalyst for liquid-phase oxidation of acetaldehyde

Catalyst for liquid-phase oxidation of acetaldehyde. Usov, Yu. N.; Zubanova, L. G.; Pletneva, E. V.; Borisova, S. V.; Ovcharov, A. G.; Doroshenko, A. P. (Saratov State University; "Nitron" Industrial Enterprises, Saratov, USSR). U.S.S.R. SU 1097371 A1 15 Jun 1984 From: Otkrytiya, Izobret., Prom. Obraztsy, Tovarnye Znaki 1984, (22), 29. (Russian). (Union of Soviet Socialist Republics). CODEN: URXXAF. CLASS: IC: B01J031-04; C07C053-12. APPLICATION: SU 82-3473638 19 Jul 1982. DOCUMENT TYPE: Patent CA Section: 45 (Industrial Organic Chemicals, Leather, Fats, and Waxes) The title catalyst with increased selectivity contains 0.003-0.03 g/L Pd acetate [19807-27-3] in addn. to 3.0-4.0 g/L Cu acetate [4180-12-5] and 1.00-2.33 g/L Co acetate [5931-89-5] in up to 1L glacial HOAc.

Continuous esterification of terephthalic acid

Continuous esterification of terephthalic acid. Takashima, Shunichi; Kawashima, Masao; Ishii, Kimiyoshi (Mitsubishi Rayon Co., Ltd., Japan). Japan. Kokai JP 52128342 27 Oct 1977 Showa, 5 pp. (Japanese). (Japan). CODEN: JKXXAF. CLASS: IC: C07C069-82. APPLICATION: JP 76-44065 16 Apr 1976. DOCUMENT TYPE: Patent CA Section: 35 (Synthetic High Polymers) Section cross-reference(s): 23, 25 The continuous esterification of terephthalic acid (I) [100-21-0] with ethylene glycol (II) [107-21-1] to bis(2-hydroxyethyl) terephthalate (III) [959-26-2] using 2 reactors in series involved (1) continuous feeding of the reactants at II/I mol ratio (a) 1.2-2.0 to the 1st reactor, (2) removing a portion or all of the II together with the esterification mixt. to the 2nd reactor to maintain a 1.05-1.3 in the 2nd reactor; the esterification was done in the presence of a Co, Mg, or Ti compd. For example, using 2 reactors, each contg. 20 kg III, a slurry from I 6.73, II 3.1, and 1% cobalt acetate [5931-89-5] soln. (in II) 0.16 kg/h were fed to the 1st reactor (dwell time 2 h, 260°, 0.5 kg/cm2 gage); 1.19 kg/h H2O and 0.65 kg/h 80% aq. II were removed from the side and bottom, resp., of the distn. tower. The esterification mixt. was fed together with the aq. II (from the 1st reactor) to the 2nd reactor (dwell time 1.6 h, 250°); 0.5 kg/h II-contg. vapor was removed from the condenser and the esterification mixt. discharged at a rate of 8.31 kg/h contained only 0.61% diethylene glycol. No oligomer accumulation was obsd. at the bottom of the distn. tower of the 1st reactor.