Zenon Environmental Inc.

Zenon Technology Partnership

Bl Technologies, Inc.

Ostara Nutrient Recovery Technologies Inc.

Other

Her Majesty the Queen As Represented by Minister of the Environment C/o

Pierre Lucien Cote

Steven Kristian Pedersen

Hidayat Husain

Arnold Frederic Janson

Henry Behmann

Manwinder Singh

Hamid R Rabie

Jeffrey Gerard Peeters

Nicholas Adams

Ian Alexander Pottinger

Nicholas William H Adams

Jason Cadera

Ian Glenn Towe

Deonarine Phagoo

Christopher J Lipski

Rhonda Maria Hyslop

William A Bonkoski

Youngseck Hong

Minggang Liu

Timothy Michael Pickett

Hadi Husain

Wajahat Hussain Syed

Ahren Britton

Ram Prasad Melahalli Sathyanarayana

Boris Fernandes Ginzburg

Francois Yacoub

Roger P Maurion

Geert-Henk Koops

James John Royston

Ake A Deutschmann

Ahren Thomas Britton

John David Ireland

Donald R Clark

Carlos F Rodrigues

Jinhua Bai

Denis Guibert

Bradley M Smith

Nicholas William Harcsar Adams

Steven Pederson

Steven Ian Low

Hamld R Rabie

Boris Fernandez Ginzburg

Nicholas William Adams

Ram Prasad Sathyanarayana

Ian G Towe

A cord for supporting a biofilm has a plurality of yarns. At least one of the yarns comprises a plurality of hollow fiber gas transfer membranes. At least one of the yarns extends along the length of the cord generally in the shape of a spiral. Optionally, one or more of the yarns may comprise one or more reinforcing filaments. In some examples, a reinforcing yarn is wrapped around a core. A module may be made by potting a plurality of the cords in at least one header. A reactor may be made and operated by placing the module in a tank fed with water to be treated and supplying a gas to the module. In use, a biofilm covers the cords to form a membrane biofilm assembly.

Membrane assembly for supporting a biofilm

This specification describes a membrane aerated biofilm media and reactor (MABR) having a discontinuous layer of a porous material applied to the outer surface of a gas-transfer membrane. The porous material may have a void fraction of 50% or more. The porous material may have a thickness of up to about 500 microns and a pattern on the same order of magnitude as its thickness. The media may be used to carry on a deammonification reaction. In use, ammonia oxidizing bacteria (AOB) and annamox bacteria grown in or on the media, with the annamox bacteria located primarily in the porous material. The supply of oxygen through the gas-transfer membrane is limited to suppress the growth of nitrite oxidizing bacteria (NOB). Excess biofilm is removed, for example by coarse bubble scouring. The media may be placed in an anoxic zone of an activated sludge plant, which may be upstream of an aerobic zone.

MABR media for supporting AOB and annamox bacteria and process for deammonification of wastewater

A method for treating phosphate-containing wastewater, such as phosphogypsum pond water. The method includes the steps of: (a) adding a first cation to the wastewater to precipitate fluorosilicate from the wastewater; (b) adding a second cation to the wastewater to precipitate fluoride from the wastewater; (c) raising the pH of the wastewater to precipitate the second cation from the wastewater; (d) removing residual silica from the wastewater; and (e) precipitating phosphate from the wastewater. The precipitated fluorosilicate may be sodium fluorosilicate. The precipitated phosphate may be struvite.

Treatment of phosphate-containing wastewater with fluorosilicate and phosphate recovery

Wastewater is treated though primary treatment of the water by way of a micro-sieve to produce a primary effluent and primary sludge. There is secondary treatment of the primary effluent by way of a membrane bioreactor (MBR) or an integrated fixed film activated sludge (IFAS) reactor to produce a secondary effluent and a waste activated sludge. The micro-sieve may have openings of 250 microns or less, for example about 150 microns. In a process, a gas transfer membrane is immersed in water. Pressurized air flows into the gas transfer membrane. An exhaust gas is withdrawn from the gas transfer membrane and used to produce bubbles from an aerator immersed in the water.

Wastewater treatment with primary treatment and MBR or MABR-IFAS reactor

An apparatus has a plurality of gas transfer membranes. The apparatus floats in water with the membranes submerged in the water. To treat the water, a gas is supplied to the membranes and is transferred to a biofilm supported on the membranes or to the water. Gas is also used to supply mixing or membrane scouring bubbles to the water. The mixing or scouring bubbles can be provided by a cyclic aeration or other gas supply system, which optionally provides gas at a variable pressure to the membranes in parallel or series with an aerator. Condensates can be removed from the membranes, and exhaust gasses from the membranes can be monitored, optionally through one or more dedicated pipes.

Process for water treatment using membrane biofilm reactor

A conventional media filter such as a gravity sand filter is converted into a membrane filter. The media is removed and replaced by immersed membrane modules. Transmembrane pressure is created by a static head pressure differential, without a suction pump, thereby creating a membrane gravity filter (MGF). Preferred operating parameters include transmembrane pressure of 5-20 kPa, 1-3 backwashes per day, and a flux of 10-20 L/m/h. The membranes are dosed with chlorine or another oxidant, preferably at 700 minutes*mg/L as Clequivalent per week or less. The small oxidant does is believed to provide a porous biofilm or fouling layer without substantially removing the layer. The media filter may be modified so that backwash wastewater is removed from near the bottom of the tank rather than through backwash troughs above the membrane modules. Membrane integrity testing may be done while the tank is emptied after a backwash.

Conversion of media filter into membrane gravity filter

A bioreactor has a biofilm that receives a gas through a supporting membrane and another biofilm attached to an inert support. The first biofilm is aerated through the membrane and provides nitrification. The other biofilm has an anoxic or anaerobic zone and provides denitrification. A module useful in the bioreactor has cords potted in at least one potting head. Optionally, some or all of the cords have a gas transfer membrane. The module may provide inert supports, active gas transfer supports or a combination of both types of support. Multiple modules may be assembled together into a cassette, the cassette providing inert supports, active supports or a combination. The module or cassette may have an aerator for mixing or biofilm control.

Assembly for supporting mixed biofilm

A method for treating, and recovering phosphate compounds from, phosphate-containing wastewater. The method includes the steps of: (a) removing fluoride from the wastewater; (b) recovering a phosphate compound from the wastewater by maintaining supersaturation conditions for the phosphate compound; and (c) polishing the wastewater. A silica removal step may be optionally performed after step (a) and before step (b).

Treatment of phosphate-containing wastewater

A method for treating, and recovering phosphate compounds from, phosphate-containing wastewater. The method includes the steps of: (a) removing fluoride from the wastewater; (b) recovering a phosphate compound from the wastewater by maintaining super saturation conditions for the phosphate compound; and (c) polishing the wastewater. A silica removal step may be optionally performed after step (a) and before step (b).

An immersed membrane system or process may use measured or calculated process information to optimize one or more process operating parameters to improve performance or reduce operating costs. An on-line process control system or method may use the resistance in series method in operating an immersed membrane water treatment system. A process control system or process may consider resistance values and adjust operational parameters such as membrane aeration frequency factor, membrane aeration flow, permeate flux, permeation duration, backwash flow and duration, relaxation duration or maintenance or recovery chemical cleaning frequencies in order to reduce the operational costs related to membrane fouling removal.

Real-time process control for an immersed membrane filtration system using a control hierarchy of discrete-state parameter changes

Various methods of making a reinforced membrane, devices for making the membranes, and the resulting membranes are described. The methods typically provide a reinforcing structure that includes filaments extending around the circumference of the membrane but without the filaments being part of a braided or woven structure. Some of the reinforcing structures also include longitudinal filaments. The methods and devices can be used to make a supporting structure in line with membrane formation steps, and also allow for a reinforced membrane to be produced that has a ratio of inside-to-outside diameters of 0.5 or more.

Non-braided, textile-reinforced hollow fiber membrane

Growing community of inventors

Dundas, Canada

Pierre Lucien Cote