Catalyst comprising platinum-tin on a silicon-containing support for the production of ethanol by hydrogenation of acetic acid
A hydrogenation catalyst, catalyst technology, applied in physical/chemical process catalysts, metal/metal oxide/metal hydroxide catalysts, catalyst activation/preparation, etc., can solve non-selectivity, hinder commercial viability, insufficient catalyst lifespan and other issues
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[0120] 1 The preparation of the individual catalysts is described in detail herein. Figures in parentheses indicate the actual component (metal, metal oxide) amount in % by weight.
[0121] 2 Product selectivities (wt %) were calculated from authentic samples corrected by GC analysis.
[0122] 3 Acetic acid conversion (%) was calculated as follows: [HOAc] conversion, %={[HOAc](feed, mmol / min)-[HOAc](effluent, mmol / min) / [HOAc](feed , mmol / min)}*100.
[0123] 4 The main product obtained with this catalyst was diethyl ether (EtOEt) with a selectivity of 96% and a yield of 2646 g / kg / h.
[0124] Compared with KA160 (SiO 2 -5%Al 2 o 3 ) and KA160-CaSiO 3 A clear shift in selectivity to ethanol was observed for the promoted catalyst. See entries 2, 6 and 7 in Table A, although at 84% this catalyst is still less selective than SiO 2 -CaSiO 3 The selectivity observed for the base material, but the conversion of acetic acid remained at 43%, was on SiO 2 -CaSiO 3 Almost tw...
Embodiment 1
[0221] In a tubular reactor made of stainless steel with an internal diameter of 30 mm and capable of being raised to a controlled temperature, 50 ml of the catalyst prepared as described in Catalyst Preparation C above were placed. The total length of the catalyst bed after charging is approximately about 70 mm.
[0222] The feed liquid consists essentially of acetic acid. The reaction feed liquid was evaporated at a temperature of 250° C. and a pressure of 100 psig and flowed for 2500 hr with hydrogen and helium as a carrier gas. -1 The average total gas hourly space velocity (GHSV) of the reactor was charged. The feed stream contains from about 6.1% to about 7.3% mole percent acetic acid and from about 54.3% to about 61.5% mole percent hydrogen. A portion of the vapor effluent from the reactor was passed through gas chromatography to analyze the content of the effluent. The selectivity to ethanol was 93.4% at 85% conversion of acetic acid.
[0223] The catalyst utilized...
Embodiment 2
[0225] The catalyst utilized was 1 wt % platinum and 1 wt % tin on calcium silicate prepared according to the procedure of Example C.
[0226] 2,500hr at a temperature of 250°C and a pressure of 22bar -1 Feedstream of vaporized acetic acid and hydrogen at average gross gas hourly space velocity (GHSV) The procedure given in Example 1 was essentially repeated. A portion of the vapor effluent was passed through gas chromatography to analyze the content of the effluent. The conversion rate of acetic acid is greater than 70%, and the selectivity of ethanol is 99%.
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