Membrane filtration device and process

• US 20060091074A1
• Filed: 09/26/2005
• Published: 05/04/2006
• Est. Priority Date: 11/23/1998
• Status: Abandoned Application

• Current Assignee: Zenon Technology Partnership
• Original Assignee: Zenon Environmental Incorporated
• Inventors: Janson, Arnold, Cote, Pierre, Pedersen, Steven, Cadera, Jason, Adams, Nicholas William H.
• Application Number:
  US11/234,186
• Publication Number:
  US 20060091074A1
• Time in Patent Office: Days
• US Class Current: 210/636
• CPC Class Codes: B01D 2311/04 Specific process operations in the feed stream; Feed pretreatment
• CPC Class Codes: B01D 2311/13 Use of sweep gas
• CPC Class Codes: B01D 2311/16 Flow or flux control
• CPC Class Codes: B01D 2311/25 Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
• CPC Class Codes: B01D 2313/08 Flow guidance means within the module or the apparatus
• CPC Class Codes: B01D 2313/12 Specific discharge elements
• CPC Class Codes: B01D 2313/21 Specific headers, end caps
• CPC Class Codes: B01D 2313/56 Specific mechanisms for loading the membrane in a module
• CPC Class Codes: B01D 2315/06 Submerged-type; Immersion type
• CPC Class Codes: B01D 2321/02 Forward flushing
• CPC Class Codes: B01D 2321/04 Backflushing
• CPC Class Codes: B01D 2321/185 Aeration
• CPC Class Codes: B01D 61/145 Ultrafiltration
• CPC Class Codes: B01D 61/146 comprising multiple ultrafiltration steps
• CPC Class Codes: B01D 61/147 Microfiltration
• CPC Class Codes: B01D 61/149 Multistep processes comprising different kinds of membrane processes selected from ultrafiltration or microfiltration
• CPC Class Codes: B01D 61/16 Feed pretreatment
• CPC Class Codes: B01D 61/18 Apparatus therefor
• CPC Class Codes: B01D 61/22 Controlling or regulating
• CPC Class Codes: B01D 63/02 Hollow fibre modules
• CPC Class Codes: B01D 63/024 : with a single potted end
• CPC Class Codes: B01D 63/031 : Two or more types of hollow fibres within one bundle or within one potting or tube-sheet
• CPC Class Codes: B01D 63/04 : comprising multiple hollow fibre assemblies
• CPC Class Codes: B01D 63/043 : with separate tube sheets
• CPC Class Codes: B01D 63/16 : Rotary, reciprocated or vibrated modules
• CPC Class Codes: B01D 65/02 : Membrane cleaning or sterilisation ; Membrane regeneration
• CPC Class Codes: B01D 65/08 : Prevention of membrane fouling or of concentration polarisation
• CPC Class Codes: B01D 65/102 : Detection of leaks in membranes
• CPC Class Codes: B01D 65/104 : Detection of leaks in membrane apparatus or modules
• CPC Class Codes: C02F 1/444 : by ultrafiltration or microfiltration
• CPC Class Codes: C02F 3/1273 : Submerged membrane bioreactors
• CPC Class Codes: Y02W 10/10 : Biological treatment of water, waste water, or sewage

Abstract

An element for use in ultrafiltration or microfiltration of potable water has a large number of small diameter hollow fibre membranes attached between two headers. Side plates attached to the sides of the headers define vertical flow channels containing the membranes. The elements may be placed side by side and stacked on top of each other to form cassettes having continuous vertical flow channels through the entire cassette. The membrane modules or cassettes may be arranged to cover a substantial part of the cross sectional area of an open tank. Tank water may flow upwards or downwards through the flow channels. A tank may be deconcentrated by at least partially emptying and refilling the tank with fresh water while permeation continues. Excess tank water created during deconcentration may flow generally upwards through the modules and out through a retentate outlet or overflow at the top of the tank.

Claims

1. A process for filtering water comprising the steps of:

(a) maintaining a level of water in a tank above a first level so as to immerse membranes while filtered permeate is withdrawn through the membranes;

(b) stopping the flow of feed water while continuing to permeate to reduce the level of water in the tank to a second level below the first level; and

(c) backwashing the membranes.

2. The process of claim 1 wherein the second level is such that the backwash causes an amount of water to overflow out of the tank to give a desired recovery rate.

3. A filtering reactor comprising:

a) an open tank;

b) a plurality of filtering membranes occupying substantially all of the horizontal cross-sectional area of the tank, to withdraw a filtered permeate;

c) an inlet to add feed to the tank from below the membranes; and

,

d) an outlet to discharge water from the tank containing retained solids.

4. A process for filtering water comprising the steps of,

a) providing a filtering reactor comprising,

i) a tank at ambient pressure;

ii) one or more modules of suction driven filtering membranes in the tank for withdrawing a filtered permeate;

iii) an inlet to add feed water to the tank; and

,

iv) retentate outlet to discharge water containing retained solids from the tank;

wherein

v) the one or more modules may be backwashed with a liquid comprising permeate;

vi) the one or more modules have a surface area of at least 500 square meters for every square meter of horizontal cross-sectional area of the tank;

vii) the one or more modules cover more than 90% of the horizontal cross-sectional area of the tank;

viii) the one or more modules are divided into elements, each element having a pair of opposed headers;

ix) the elements are separated from each other by impervious plates; and

,

x) channels are provided for water to flow vertically through the elements;

b) in repeated cycles,

(i) permeating filtered water while adding a sufficient volume of feed water to the tank to keep the membranes submerged; and

(ii) performing a deconcentration step further comprising at least one or both of (A) providing a flow of feed water into the tank from below the modules or (B) backwashing the one or more membrane modules with a liquid comprising permeate, wherein excess water containing retained solids flows out of the retentate outlet.

5. The process of claim 4 wherein the step of permeating is performed at a flux of less than 60 Liters per square meter per hour based on the surface area of the outside of the filtering membranes.

6. The process of claim 4 wherein permeation is stopped during the deconcentration step and the one or more modules are aerated while permeation is stopped during the deconcentration step.

7. A filtration apparatus comprising,

(a) an element of filtering hollow fiber membranes having,

(i) a pair of opposed horizontally spaced, vertically extending solid bodies;

(ii) a plurality of hollow fibre membranes attached to and suspended between the pair of solid bodies, the hollow fibre membranes having each at least one open end and an outer surface, the outer surfaces of the open ends of the hollow fibre membranes connected to at least one solid body with a water impermeable connection; and

,

(iii) one or more permeate channels in at least one of the solid bodies in fluid communication with the interior of the hollow fibre membranes for collecting a permeate drawn through the hollow fibre membranes;

(b) a vessel for holding water to be filtered;

(c) a structure for restraining the element in the vessel wherein the restraint provided by the vessel releasable in a direction substantially normal to the headers of the element.

8. The apparatus of claim 7 wherein the structure includes horizontally oriented racks having a bearing surface to slidably support the element and an opening to allow water to flow vertically through the rack.

9. The apparatus of claim 7 wherein the element has a releasable and resealable water tight fitting between the element and a permeate collector, the releasable and resealable water tight fitting being releasable by moving the element in the direction substantially normal to the headers of the element and resealable by moving the element in a reverse direction.

10. The apparatus of claim 7 further comprising an aerator below the element.

11. The apparatus of claim 8 wherein the rack has a stop and a releasable catch.