Fluid treatment systems and components are provided for a removal of solid matter from water or other fluids in which a chemical or chemicals may be introduced into the fluid under pressure to coagulate and/or conglomerate the solid materials and cause them to be dropped out of the treatment system and be removed. The fluid treatment system can include: an equalization chamber receiving a wastewater; a clarification chamber receiving a partially separated water from the equalization chamber; a mixing tube having an inlet end and an outlet end; and a sludge detector.

An elongate diffuser is disclosed comprising a diffuser body and a membrane attached to the diffuser body. The membrane is connected to the diffuser body so that introduction of gas at a working pressure into the diffuser displaces part of the membrane from contact with the diffuser body to provide an elongate sealed compartment between the membrane and a surface of the diffuser body. The compartment has a first lateral side interface region where the membrane contacts the diffuser body, a laterally intermediate region where the membrane is spaced apart from the diffuser body and a second lateral side interface region where the membrane contacts the diffuser body. The diffuser body surface which bounds the compartment comprises a recessed portion which is recessed away from the membrane between the first second lateral side interface regions.

A hydro turbulator system includes a volute that has a top duct and a bottom duct that allow fluid to enter and exit the volute. An impeller system including a first impeller and a second impeller is positioned within the volute. The first impeller and the second impeller are axially aligned. A motor is operationally connected to the impeller system so that the first impeller and the second impeller rotate upon operation of the motor. Rotation of the first impeller and the second impeller creates successive zones of high pressure and low pressure to agitate and condition fluid within the volute.

An all-ceramic diffuser supplies microbubbles of a narrow range of size to create a steady flow of bubbles of generally uniform size in an aqueous medium, such as process water in a wastewater treatment plant. The diffuser is formed of a porous body core, with pore sizes of e.g. 30 .Math.m or larger, an upper ceramic membrane that covers the upper surface of the body core, and has mean pore size of e.g., 3 to 15 .Math.m. A lower ceramic membrane covers the bottom surface of the body core, and has a finer pore size than the upper ceramic membrane, so that the capillary pore size of the smaller pores will act as a seal; consequently all of the air flow is through the upper ceramic membrane. A ceramic fitting connects the associated air supply with the porous body core which serves as plenum.

There is provided an ammonia gas removal system, including a fine bubble generation device which is configured to receive at least a portion of scrubber process water from a storage tank, and to generate fine bubbles containing carbon dioxide gas in the received scrubber process water, the storage tank being configured to store the scrubber process water to be provided to a gas scrubber, the gas scrubber being configured to spray the process water onto ammonia-containing gas.

A floating aerator that is highly efficient in oxygenating water and wastewater utilizes high-volume, low pressure air that is diffused into a sub-surface oxygen transfer chamber in which water and wastewater is oxygenated. An air lift is created in the oxygen transfer chamber through the discharge of air bubbles in the water column in the aerator. The aerator comprises a floating head having a concave lower surface, a main chamber or barrel that defines the oxygen transfer chamber, and an air diffuser that extends coaxially through the float head and barrel interconnects the float head to the barrel such that there is a discharge slot defined between the lower surface of the float head and the barrel. A ballast ring floats the aerator at the desire level such that a flow of air bubbles and oxygenated water or wastewater are discharged at a subsurface level.

This application relates to a method of treating wastewater wherein an oxygen infusion system is used to supersaturate wastewater before aerobic biological processes, wherein oxygen is transferred to the wastewater free of oxygen bubbles and achieves a reduction in power demand for the aeration process of wastewater.

A diffusion system comprising an upper unit and a lower unit. The upper unit comprises a series of tubing that is situated so as to effectuate collision of the fluid and air molecules. The upper unit uses vortex winding and unwinding and pressure gradients to avoid gas and liquid separation to accomplish successful collisions between a gas and a liquid. The lower unit comprises a filtering system, liquid intake system, air intake system, and submersible liquid transportation system.

The present invention concerns a nozzle for injecting pressurized water containing a dissolved gas, said nozzle comprising: a cylindrical intake chamber (20) for said water; a cylindrical expansion chamber (30) comprising a part (301) communicating with said intake chamber (20) by an orifice (401) and an outlet; a diffusion chamber (60) of truncated conical section communicating with the outlet of said expansion chamber (30) and widening out from said expansion chamber;
said nozzle comprising means for putting the stream of water that flows out of said expansion chamber (30) into rotation.

The invention relates to a method for controlling a flow generator (1) in a tank (20) configured for housing a liquid comprising solid matter, the flow generator (1) comprising an impeller and being located at a height (h-mixer) in the tank (20) and the tank (20) having a predetermined maximum filling height (h-max), wherein the flow generator (1) is configured to be operated at a variable operational speed (n) and the demand of operational speed (n-demand) is dependent on the present liquid level height (h-present) in the tank (20), wherein a max operational speed (n-max) of the flow generator (1) is the operational speed required when the liquid level in the tank (20) is equal to the maximum filling height (h-max), the present operational speed (n-present) being set equal to the demand of operational speed (n-demand) of the flow generator (1) that is determined using the formula:

[00001]$\left(n-\mathrm{present}\right)=\left(n-\mathrm{demand}\right)=\frac{\left(n-\max \right)}{\left[\left(h-\max \right)/\left(h-\mathrm{present}\right)\right]^a}$

at least when [(h-mixer)+X]≤(h-present)≤(h-max), wherein a≥(¼) and a<1, X=radius of the impeller of the flow generator+1, and all heights and measures are given in meter.