Advanced

Optimisation of membrane area and energy requirement in tubular membrane modules

Nordin, Anna-Karin LU and Jönsson, Ann-Sofi LU (2006) In Desalination 199(1-3). p.94-95
Abstract
During ultrafiltration (UF), the driving force along the membrane is diminished due to concentration increase and frictional pressure drop. In most applications of ultrafiltration the influence of the frictional pressure drop is negligible. However, when treating concentrated, viscous liquids the frictional pressure drop can reduce the transmembrane pressure (TMP) significantly. The influence of cross-flow velocity and inlet pressure on flux and frictional pressure drop during concentration of retentate from the Stora Enso Nymölla pulp and paper mill ultrafiltration plant treating hardwood bleach plant effluent was studied in this work. The experimental data were used in a calculation tool to investigate the membrane area and energy... (More)
During ultrafiltration (UF), the driving force along the membrane is diminished due to concentration increase and frictional pressure drop. In most applications of ultrafiltration the influence of the frictional pressure drop is negligible. However, when treating concentrated, viscous liquids the frictional pressure drop can reduce the transmembrane pressure (TMP) significantly. The influence of cross-flow velocity and inlet pressure on flux and frictional pressure drop during concentration of retentate from the Stora Enso Nymölla pulp and paper mill ultrafiltration plant treating hardwood bleach plant effluent was studied in this work. The experimental data were used in a calculation tool to investigate the membrane area and energy requirement of two module design alternatives during concentration of the retentate in an additional stage. The first alternative is the same module design as in the existing plant on the hardwood line at Nymölla, where the tubular membranes in a module are connected in series. In the second alternative, the membrane tubes in a module were instead connected in parallel.



The experimental flux increased markedly with increasing pressure and cross-flow velocity at all concentrations. However, the flux was significantly reduced when the chemical oxygen demand (COD) was increased. The flux was 120 l/m2 h at 180 g/l and 23 l/m2 h at 330 g/l (at 1.0 MPa and 4 m/s). The concentration was 180 and 330 g/l at volume reduction factor (VRF) 1 and 2. The calculated average flux was significantly higher in the design with membrane tubes in parallel. In addition, the flux was not only higher, but it also increased with increasing cross-flow velocity, whereas the flux in the design with membrane tubes in series reached a maximum flux at about 3 m/s. (Less)
Please use this url to cite or link to this publication:
author
organization
publishing date
type
Contribution to journal
publication status
published
subject
keywords
Ultrafiltration, Bleach plant effluent, Energy requirement, Tubular membranes
in
Desalination
volume
199
issue
1-3
pages
94 - 95
publisher
Elsevier
external identifiers
  • wos:000242275900037
  • scopus:33746701911
ISSN
1873-4464
DOI
10.1016/j.desal.2006.03.022
language
English
LU publication?
yes
id
edda1463-009d-4f53-b8a4-388aeeaa3b98 (old id 685613)
date added to LUP
2016-04-01 12:00:07
date last changed
2019-02-20 04:06:05
@article{edda1463-009d-4f53-b8a4-388aeeaa3b98,
  abstract     = {During ultrafiltration (UF), the driving force along the membrane is diminished due to concentration increase and frictional pressure drop. In most applications of ultrafiltration the influence of the frictional pressure drop is negligible. However, when treating concentrated, viscous liquids the frictional pressure drop can reduce the transmembrane pressure (TMP) significantly. The influence of cross-flow velocity and inlet pressure on flux and frictional pressure drop during concentration of retentate from the Stora Enso Nymölla pulp and paper mill ultrafiltration plant treating hardwood bleach plant effluent was studied in this work. The experimental data were used in a calculation tool to investigate the membrane area and energy requirement of two module design alternatives during concentration of the retentate in an additional stage. The first alternative is the same module design as in the existing plant on the hardwood line at Nymölla, where the tubular membranes in a module are connected in series. In the second alternative, the membrane tubes in a module were instead connected in parallel.<br/><br>
<br/><br>
The experimental flux increased markedly with increasing pressure and cross-flow velocity at all concentrations. However, the flux was significantly reduced when the chemical oxygen demand (COD) was increased. The flux was 120 l/m2 h at 180 g/l and 23 l/m2 h at 330 g/l (at 1.0 MPa and 4 m/s). The concentration was 180 and 330 g/l at volume reduction factor (VRF) 1 and 2. The calculated average flux was significantly higher in the design with membrane tubes in parallel. In addition, the flux was not only higher, but it also increased with increasing cross-flow velocity, whereas the flux in the design with membrane tubes in series reached a maximum flux at about 3 m/s.},
  author       = {Nordin, Anna-Karin and Jönsson, Ann-Sofi},
  issn         = {1873-4464},
  language     = {eng},
  number       = {1-3},
  pages        = {94--95},
  publisher    = {Elsevier},
  series       = {Desalination},
  title        = {Optimisation of membrane area and energy requirement in tubular membrane modules},
  url          = {http://dx.doi.org/10.1016/j.desal.2006.03.022},
  doi          = {10.1016/j.desal.2006.03.022},
  volume       = {199},
  year         = {2006},
}