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Recent research has focused on the use of continuous reactor systems such as membrane, fixed bed and microreactors.
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These computations were performed in three steps representing the use of continuous reactors in series reported by Grootjen et al. (1991) [ 45].
In earlier studies, we described a one-dimensional rotary reactor model, and used it to demonstrate the feasibility of continuous reactor operation.
The feasibility of thermo-chemical destruction of polychlorinated biphenyls (PCBs) was investigated using a batch reactor and two different (vertical and horizontal) types of continuous reactor.
Traditional methanization approaches, such as the use of continuous stirred tank reactor (CSTR), require long residence times in order to meet the slow (rate limiting) hydrolysis step and to prevent the loss of slowly growing microorganisms.
The use of continuous flow structured reactors for the oxidation of glycerol under mild conditions using a gold/carbon catalyst is demonstrated.
An enzyme, creating a high degree of hydrolysis in short time, was required for the use in the continuous reactor system.
Whereas isobutanol is produced industrially via carbonylation (incorporation of carbon monoxide into organic compounds) of propylene or hydrogenation of isobutyraldehyde using an enclosed continuous reactor, isobutanol is naturally produced in negligible amounts by Saccharomyces cerevisiae as a degradation product of valine.
Liquid-phase hydrogenation of acetophenone over a Rh/C catalyst has been performed using both continuous reactors.
Using acid-catalyzed esterification, a continuous reactor, containing four separate continuous stirred tank reactors (CSTR's), was designed and used to reduce the free fatty acid (FFA) content of mixed crude palm oil (MCPO).
The use of conventional continuous stirred tank reactor (CSTR) can affect the methane (CH4) recovery in a two-stage anaerobic digestion of food waste (FW) due to carbon short circuiting in the hydrolysis acidogenesis (Hy Aci) stage.
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