The similar result was reported previously (Ma et al.,
2012), which was because the NH3–N molecule size is too small
to be removed by the physical rejection of membrane.
The VFA of the bioreactor effluent increased with the organic
load from 450 to 1000 mgHAc/L on days 0–80 (Fig. 2(C)) and stabilized at 900–1000 mgHAc/L in the following 50 days. On day 130,
the VFA decreased to 800 mgHAc/L, where it remained until the
start-up phase was complete. VFA rejection was also observed
throughout the whole stage, which caused a decrease in the VFA
and an increase in the pH from the bioreactor effluent to the final
permeate. The influent pH was kept at 7.0 initially, and the pH of
the bioreactor effluent increased steadily to a maximum value of
8.0 on day 110, which was unsuitable for anaerobic operations
(Rao and Bapat, 2006). In the following days, the influent pH was
adjusted to 6.3, and the pH in bioreactor effluent decreased to an
appropriate value (7.4).
The similar result was reported previously (Ma et al.,2012), which was because the NH3–N molecule size is too smallto be removed by the physical rejection of membrane.The VFA of the bioreactor effluent increased with the organicload from 450 to 1000 mgHAc/L on days 0–80 (Fig. 2(C)) and stabilized at 900–1000 mgHAc/L in the following 50 days. On day 130,the VFA decreased to 800 mgHAc/L, where it remained until thestart-up phase was complete. VFA rejection was also observedthroughout the whole stage, which caused a decrease in the VFAand an increase in the pH from the bioreactor effluent to the finalpermeate. The influent pH was kept at 7.0 initially, and the pH ofthe bioreactor effluent increased steadily to a maximum value of8.0 on day 110, which was unsuitable for anaerobic operations(Rao and Bapat, 2006). In the following days, the influent pH wasadjusted to 6.3, and the pH in bioreactor effluent decreased to anappropriate value (7.4).
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