Patent Application
20140076787
The present invention relates to methods and apparatus for separating dissimilar materials; more particularly, to such separating by gas-assisted gravitational flotation; and most particularly, to a method and apparatus for separating by a plurality of dissimilar particulate solid and liquid materials, dispersed in a fluid medium, by controlled generation of gas bubbles in situ, defined herein as chemically-induced sparging.
It is known in the prior chemical engineering arts to separate particulate materials, such as globules of bitumen from inorganic particulates such as sand or silt dispersed in a water medium (also referred to herein as a “slurry”), by flotation in a tank. Typically, the bitumen globules tend to rise to the surface and the sand or silt particles tend to sink because of differences in specific gravity. The separation can be assisted by sparging of bubbles of air or other gases over the bottom of the tank wherein the inherent buoyant rise of the bubbles helps to sweep the bitumen globules upward through the slurry. These bubbles are not generated in situ but rather result from gas that is piped into the tank from an external source, typically through a device known generally as a sparger which is provided with a plurality of very small through which the gas enters the slurry below the surface. In general in the prior art, a not entirely satisfactory way has been found to control the characteristics of bubble populations by the sparging method. The formation of bubbles, and the size range of the bubbles generated, are controllable typically by selecting the pore size of the sparger and varying the temperature of the slurry, the height of the slurry column, and the gas flow rate. Typically, a relatively wide range of bubble diameters is produced. Exemplary particulates separated by such sparging and flotation in the prior art are mineral ores and bitumen globules derived from tar sands.
A typical prior art gas flotation cell is available from Outotec Pty, Ltd in Australia.
The gas phase of any flotation cell is critical for optimum cell performance. Understanding and being able to vary the four key parameters in the gas phase can bring real results—with over 30% recovery improvement at the same grade, in one particular case. The recovery in a flotation cell is directly related to the amount of air added to the cell. Therefore there is a minimum air requirement for a given number of solid particles, below which efficient flotation cannot take place.
The method by which the air is added to the flotation cell in the prior art is also vitally important as it controls the size of the bubbles generated and the flow patterns in the cell. The flotation rotor and stator and the separation vessel must provide sufficient turbulence for bubble-particle collisions to occur and be able to generate bubbles in a certain size range depending on the particle size to be floated. The correct flow patterns up the cell of particles and bubbles must then be formed so that the particles are carried up to the froth phase without significant dropback occurring. In other words, if the gas phase is not handled properly, chances are the flotation cell is not performing as well as it could be.
There are several of gas phase parameters that can be directly measured and used to optimize the performance of this phase. Typically the gas phase can be described by four parameters:
1. Gas hold-up
2. Bubble size and bubble size distribution
3. Superficial gas velocity
4. Bubble surface area flux.
Gas hold-up (eg) is the volume of the gas in the flotation cell's slurry zone. The volume of gas reduces the slurry volume and therefore decreases the residence time available for flotation. The gas holdup depends on the amount of gas, typically in the form of atmospheric air, added to the cell and is a strong function of slurry viscosity. Typically, gas holdup is limited to between 5% and 15% of the total slurry volume, to maximize the cell volume and residence time.
Bubble size and its distribution (db) in a cell's slurry zone directly affect the particle/bubble interactions and hence flotation performance. For optimal performance, it is critical to generate bubbles of the correct diameter based on the size of particles to be floated. Smaller bubbles are generally required for fine particle flotation and larger bubbles for coarse particle flotation.
Example: 1 m3 of air contains approximately 566 million bubbles of 1.5 mm diameter. At an aeration rate of 20 m3/min, 189 million bubbles/sec must be generated. Similarly, 1 ton of typical solids contains 1 billion (spherical particles) of 70 microns in size (after grinding). At a solids feed rate of 300 ton/hour, 83 million particles are generated per second. Of these 83 million particles/second, approximately 10% are collected in a rougher duty, 50% in a cleaner duty, and 85% in a recleaner duty. This corresponds to 2.3 bubbles per particle. This may seem sufficient; however, due to issues such as poor liberation, incorrect reagent addition, slurry chemistry, and oxidation, flotation recoveries of 100% are never achieved. If the bubble diameter were 2.0 mm, there would only be 80 million bubbles/second, which would reduce the number of bubbles per particle to fewer than one.
The bubble size and bubble size distribution can be measured in each flotation cell using a photographic Bubble Sizer. A sample of bubbles is photographed with a digital still camera and an automated image analysis procedure is used to size the collected bubbles from the digital images.
There are two main methods of calculating the average bubble diameter of a distribution. The first is to calculate the average of all bubble diameters in the distribution (known as the average bubble diameter d10). The second is to calculate the sum of all bubbles' volume divided by the sum of all bubbles' surface area (known as the Sauter mean bubble diameter d32). The Sauter mean bubble diameter is always larger than the average bubble diameter as it takes more account of large bubbles with large volumes; therefore it is a better measure of bubble size.
A known commercially-available flotation mechanism is able to produce small bubbles with average bubble diameters between 1.0 mm and 1.5 mm and Sauter mean bubble diameters between 1.5 mm and 2.0 mm.
Superficial gas velocity (Jg) is the bubble's upward velocity relative to the cell cross-sectional area. It is proportional to the air addition rate and can indicate local flow patterns and gas short-circuiting. Excessive air addition increases bubble size, as the mechanism is unable to disperse the air, and is therefore detrimental to flotation performance. Controlling the air rate within an optimal range is very important.
The average rise velocity of bubbles in the flotation cell can be measured in combination with the bubble size measurements from the Bubble Sizer. A closed cylinder connected above the viewing chamber is filled with water before the bubble sizing takes place. During the bubble size measurement, the water in the cylinder is displaced by the rising air bubbles and the water level drops. The time taken (t) for the water level to fall a known distance, L, is measured and the superficial gas velocity calculated from the following equation:
Jg=Lt
Adjustments are then made to account for the pressure difference between the location of the sampling valve and where the measurement is made in the cylinder.
Typical superficial gas velocities are between 0.5 cm/sec and 1.5 cm/sec. As the air rises into the froth zone, the superficial gas velocity increases with decreasing surface area in the froth zone.
Superficial gas velocity measurements performed radially across a flotation cell can provide information on the gas dispersion efficiency. It is common for the superficial gas velocity to be slightly higher in the middle of the cell due to the air addition there. As the air rate increases, the bubbles rise faster in the cell center as the mechanism becomes less efficient at air dispersion, until the air cannot be dispersed and ‘boiling’ occurs.
Measurements of superficial gas velocity can also provide information on mechanism wear. If there is, for example, an uneven distribution across the cell, the sparging stator could be worn out on one side.
Bubble surface area flux (BSAF) is the amount of bubble surface area rising up a flotation cell per cross sectional area per unit time. It depends directly on the bubble size and superficial gas velocity. At shallow froth depths, BSAF is linearly proportional to the first order flotation rate constant; generally, the greater the bubble surface area flux, the higher the recovery rate in the slurry zone of a cell. However if excessive air is added, the recovery rate in the slurry zone can decrease due to ‘boiling’.
A significant amount of test work has been performed on bubble surface area flux over the past 15 years, and the relationship between bubble surface area flux and the first order flotation rate constant has been successfully validated for prior art mechanically induced sparging and holds for cells of all sizes, from 60 litres to 300 m3. It is essentially a direct measure of pulp zone flotation efficiency.
The bubble surface area flux can be measured directly using the following equation:
Sb=6·Jg×d32
Sb=Bubble surface area flux (cm2/cm2 s)
d32=Sauter mean bubble diameter (cm)
Jg=Superficial gas velocity (cm/s)
Typically, BSAF ranges between 30 s−1 and 60 s−1 and can be varied directly by changing the air addition rate.
What is needed in the art is a method and apparatus wherein the size range of bubbles, density of bubbles (number per unit volume), and the rate of bubble generation in situ in a slurry by decomposition of a chemical agent in a process that can be controlled to desired and predetermined process aim points.
It is a principal object of the present invention to improve the rate, degree of separation, and percent recovery of particulates in a slurry by controlled chemically-induced sparging by bubbles formed in situ in the slurry.
Briefly described, a method and apparatus in accordance with the present invention utilizes a decomposable compound such as hydrogen peroxide as a primary additive to generate bubbles within a fluid medium, e.g., an aqueous slurry of particulates having differing flotation properties. Bubbles generated within the slurry by chemical decomposition of the decomposable compound. The size range of bubbles, density (number per unit volume) of bubbles, and rate of in situ generation of bubbles may be controlled by controlling process variables such as temperature, concentration and flow rate of the decomposable compound, feed rate of the slurry, percent solids of the slurry (ratio of water to solids), residence time of the decomposable compound in the presence of the particulates, pH of the slurry, and addition of one or more secondary process additives including salts. As used herein, in situ should be taken to mean within the fluid medium. Bubble generation and materials separation can occur in a primary separation cell, a secondary and tertiary separation cells, and/or an auxiliary reactor.
The present invention will now be described, by way of example, with reference to the accompanying drawings, in which:
Corresponding reference characters indicate corresponding parts throughout the several views. The exemplification set out herein illustrates one preferred embodiment of the invention, in one form, and such exemplification is not to be construed as limiting the scope of the invention in any manner.
Referring now and specifically to the flotation phenomenon, it will be seen that particulate separation by flotation in a novel process wherein bubbles are generated spontaneously by chemical decomposition within the slurry itself is fundamentally different from conventional prior art flotation processes wherein bubbles are formed by sparging of air into the slurry. This novel process is defined herein as “chemically-induced sparging”.
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Coincidentally and beneficially, salt level and pH are both in the desired range in a prior art process widely used for recovering bitumen globules from tar sands, making the present process especially useful.
An added benefit of chemically-induced sparging is that in many commercial processes there can be a wide range of ore composition and behavior, which can be accommodated immediately by adjustment of process parameters. Such accommodation is simply not possible with prior art mechanical spargers.
Referring now to
In contrast, the present process 100 is believed by the inventors to have the benefit of forming the bubbles 102 right from the molecular level right at the surface of the desired particles. As a result, and in stark contrast to the prior art, a substantial proportion of the formed bubbles remain attached 104 to the particles and act like little oxygen balloons to buoy the particles upward.
Accordingly, the prior art rules for optimum bubble formation and bubble characteristics may not be applied directly but rather must be modified in consonance with the present novel mechanism of bubble formation and flotation.
From the foregoing description it will be apparent that there have been provided improved methods and apparatus for separating dissimilar particulate materials dispersed in a fluid medium, especially for economically recovering petroleum-like hydrocarbon residues from particulate mineral substrates, especially hydrocarbonaceous ores such as tar sands, and for discharging a substrate residue environmentally suitable for landfill disposal. Variations and modifications of the herein described methods and apparatus, in accordance with the invention, will undoubtedly suggest themselves to those skilled in this art. Accordingly, the foregoing description should be taken as illustrative and not in a limiting sense.
The present application draws priority from a pending U.S. Provisional Patent Application Ser. No. 61/520,934, filed Jun. 17, 2011.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/CA12/00291 | 6/15/2012 | WO | 00 | 9/25/2013 |
| Number | Date | Country | |
|---|---|---|---|
| 61520934 | Jun 2011 | US |
