Advanced

Optimisation of membrane area and energy requirement in tubular membrane modules

Nordin, Anna-Karin LU and Jönsson, Ann-Sofi LU (2008) In Chemical Engineering and Processing 47(7). p.1090-1097
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 Nymolla 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 Nymolla 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 Nymolla, 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/m(2) h at 180 g/l and 23 l/m(2) 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
membranes, tubular, energy requirement, ultrafiltration, bleach plant effluent
in
Chemical Engineering and Processing
volume
47
issue
7
pages
1090 - 1097
publisher
Elsevier
external identifiers
  • wos:000256735700008
  • scopus:43549101574
ISSN
0255-2701
DOI
10.1016/j.cep.2007.09.010
language
English
LU publication?
yes
id
537f228b-ed3d-4891-b6e9-ffac0fab318a (old id 1200338)
date added to LUP
2008-09-12 12:27:11
date last changed
2017-01-01 05:08:17
@article{537f228b-ed3d-4891-b6e9-ffac0fab318a,
  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 Nymolla 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 Nymolla, 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/m(2) h at 180 g/l and 23 l/m(2) 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         = {0255-2701},
  keyword      = {membranes,tubular,energy requirement,ultrafiltration,bleach plant effluent},
  language     = {eng},
  number       = {7},
  pages        = {1090--1097},
  publisher    = {Elsevier},
  series       = {Chemical Engineering and Processing},
  title        = {Optimisation of membrane area and energy requirement in tubular membrane modules},
  url          = {http://dx.doi.org/10.1016/j.cep.2007.09.010},
  volume       = {47},
  year         = {2008},
}