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Meanwhile, the furnace heated up at a rate of 5 °C min−1 until complete CO conversion was reached.
During oxidation, the CO2 surface area increased by an additional 100 150 m2/g, until 50% conversion was reached.
The same conversion was reached in a LLTP-system consisting of water and β-myrcene, whereas a product yield of 55% was achieved.
In the esterification reaction, around 70% ester conversion was reached after 2 h of reaction under experimental conditions previously optimized by Central Composite Rotatable Design (CCRD).
The normal lactone (1S,5R -2-oxabicyclo[3.3.0]oct-6-en-3-one (ee > 99%) was generated in a fast reaction, and full conversion was reached after 45 min.
The fuel conversion increased with temperature for both materials and full conversion was reached above 800 °C with a fuel reactor inventory of 225 kg/MW for Fe0.66Mn1.33SiO3, while FeMnSiO3 was incapable of providing full conversion.
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The reactor operates discontinuously and its time evolution is simulated until a 90% reactant conversion is reached.
The highest glucan, xylan and arabinose conversion were reached after 72 h of hydrolysis for all tested biomasses, pretreatment methods and enzyme mixes.
Regarding the most active catalyst Dowex50Wx2, 90% of equilibrium conversion is reached after 5 min at 60 °C employing a catalyst loading of 1 wt.%.
The analysis of the effect of operation conditions (temperature, run time and alcohol/metal (A/M) ratio) on catalytic performance revealed a quite complex reaction network, in which acid formation starts only after a certain level of conversion is reached.
A typical test was conducted according to this sequence: (1) reactor heat-up from ambient to 150 °C with air to remove any possible impurities; (2) introduction of the mixed gas (1000 ppm of CO and 50 %-vol of air in N2) to the reactor; and (3) second reactor heat-up from 150 °C to the temperature at which 100%% CO conversion is reached, (TOS = 2 h at 100%% conversion).
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