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By K. C. Sclater

GAS as a factor in the efficiency of oil production, might be a better title for this paper as it deals in general with the significance of the gas-oil ratio as an index of the efficiency of oil production and briefly discusses oil production methods with reference to the gas-oil ratio in wells, particularly during the early life of a field. In the recent hearings held at Washington before the Federal Oil Conservation Board the fuller utilization of the energy contained in the gas occluded in or associated with the oil underground was stressed by some of the speakers when referring to greater ultimate recovery of oil. One speaker commenting on this point said in part, "There is ample evidence indicative that if the gas associated with the petroleum in our fields were conserved and elevated gas pressure maintained in the oil sands during their productive life, the ultimate production of oil could be greatly increased."

Jan 1, 1926

By C. A. C. Sequeira, G. N. Anastassakis

Electrochemical processes occur on nano-, micro- and macro- scale in numerous applications such as fuel cells, batteries, hydrogen production, mineral extraction, water treatment, electrotherapy, sensors and many others. In most of these applications, gases evolve either at one or both electrodes due to electrolysis. These gases form bubbles play a crucial role in electrochemical systems. For example, in electrowinning (EW) that is used to extract and refine metals such as Cu, Zn, Ni, Mn, and Cd from their solutions, in most cases the solution is acidic and oxidation of water molecules at the anode is the common counter reaction, which results in the liberation of oxygen bubbles. This generally requires a high overpotential and accounts for a considerable percentage of the energy consumed in metal EW electrolytic cells, apart from producing acid mist that is very corrosive for other cell equipment and building structures. The behaviour of bubbles in electrochemical systems is still a complex challenging topic which requires a better understanding of gas bubbles hydrodynamics and their interactions with electrode surface and bulk liquid, as well as between the bubbles themselves. The objective of the current paper is to briefly review the fundamental hydrodynamics of both gas bubbles on the electrode surface and gas bubbles interaction with the liquid bulk solution. The current work also investigates the impact of gas bubbling and some operating parameters in copper EW, such as current density (100-500 A/m2), temperature (25-75ºC), acidity (50-300 g/L) and a typical chemical mist suppressant (<50 ppm). The results clearly show that both suppressant and temperature reduced the overall surface tension of the solution. Also, chloride concentration and applied current improved electrolyte flow and copper quality at higher current densities. The current paper contributes to the development of mineral processing (specifically to copper hydrometallurgy), as it deals with fundamental hydrodynamics and interactions of gas bubbles that formed during copper EW and play a crucial role in copper electrochemical systems.

Jan 1, 2018

By P. P. Gregory

NATURAL petroleum gas occurring in the oil-bearing reservoirs is found to exist either as free gas associated with the oil and/or in solution in the oil. In some virgin fields practically no free gas is encountered under the reservoir conditions of pressure and temperature, although in other fields a considerable section of the ``pay" horizon is occupied by free gas. In other words, a given oil field may or may not have a gas cap before the exploitation takes place. However, when the reservoir pressure is reduced to a point below the critical saturation pressure by withdrawals of fluids from the producing formation, the gas dissolved in the oil inevitably begins to come out of solution and becomes free gas. Under the con-trolled methods of production and drilling, a portion of this gas is pro-duced with the oil to the surface and a portion of it remains within the reservoir to accumulate at higher structural levels toward which it migrates by virtue of its low specific gravity. The rate of growth of a gas cap in a-given structure depends primarily upon the rate of decline in the reservoir pressure. If the rate of pressure decline is rapid, the gas cap likewise will grog rapidly. On the other hand, shrinkage in the gas-cap area was noted in some fields in which reservoir pressures were increasing.

Jan 1, 1938

By T P. Fischer, S N. Williams, N C. Sturchio

Chemical and isotopic analyses of fumarole gases from Galeras Volcano, Colombia provide significant insights into the origin of volatile components in the magma. Water comprises a mixture of magmatic (rock-equilibrated at high temperature) and meteoric, with the relative proportions varying through time. Carbon isotopes are most consistent with a mantle source, although other contributions to the system cannot be ruled out. Nitrogen most likely originated from organic matter in subducted oceanic sediments. All of these &apos;primary&apos; components have been modified somewhat by interaction or exchange with other reservoirs during ascent to the surface. In addition to information on the origin of the gases, these data show significant temporal variations precursory to eruptive events. Chemical ratios change and water becomes more meteoric in character prior to eruptions.

Jan 1, 1995

By Sturchio NC, Williams SN, Fischer TP

Chemical and isotopic analyses of fumarole gases from Galeras Volcano, Colombia provide significant insights into the origin of volatile components in the magma.. Water comprises a mixture of magmatic (rock-equilibrated at high temperature) and meteoric, with the relative proportions varying through time. Carbon isotopes are most consistent with a mantle source, although other contributions to the system cannot be ruled out. Nitrogen most likely originated from organic matter in subducted oceanic sediments. All of these "primary" components have been modified somewhat by interaction or exchange with other reservoirs during ascent to the surface. In addition to information on the origin of the gases, these data show significant temporal variations precursory to eruptive events. Chemical ratios change and water becomes more meteoric in character prior to eruptions.

Jan 1, 1995

By David M. Sullivan

Jim Walter Resources, Inc., (JWR) a division of Jim Walter Corporation, has 5 underground coal mines in Central Alabama varying in depths from 400-2500 feet. Gas Chromatography plays a vital role in safety and production at each mine. Chromatographic data is used to monitor working areas for safety and proper ventilation and to control the quality of extracted methane for sales purposes. Instruments have a1 so been employed during mine rescue operations. JWR&apos;s first Gas Chromatograph (GC) was installed in April 1984 to monitor gob gas taken from longwall gob areas and sold based upon BTU value. The GC allows maximum extraction rate of the gas within the quality guidelines. By late 1985, another system was purchased and both units were upgraded to perform an analysis of indicator gases which may appear during mine emergencies. Each unit has the ability to detect and measure the following gases at almost any level ; Oxygen (021, Nitrogen (N2), Methane (CH4), Carbon Dioxide (C02), Hydrogen (HZ), Carbon Monoxide (CO) , Ethylene (C2H4), Ethane (C2H61, Acetylene (C2H2) and a composite of hydrocarbon threes and above (C3+). The analytical run is accomplished in less than ten minutes and is completely automated. This report will introduce Gas Chromatography as applied by Jim Walter Resources for the analysis of underground mine air.

Jan 1, 1987

By P. Bartel

Coal cleaning can be effected by the bacterium Sulfolobus acidocaldarius, which in oxidizing sulfur and dissolving mineral matter requires carbon dioxide and oxygen; carbon dioxide as a carbon source and oxygen as an electron acceptor. The desulfurization of coal by thermophilic bacteria under elevated partial pressures of carbon dioxide and oxygen was studied at a total pressure of 1 atm. The partial pressure of carbon dioxide was varied over the range 0.00032 to 0.33 atm (0.00032, 0.007, 0.10, 0.33 atm), and the partial pressure of oxygen was varied over the range 0.14 to 0.40 atm (0.14, 0.21, 0.30, 0.40 atm). The maximum rate of coal desulfurization increased by 32%, from 9.0 to 11.9 mg S/1 hr, as air was enriched in carbon dioxide from its atmospheric level of 0.00032 atm to 0.10 atm. Enrichment with carbon dioxide up to 0.10 atm, at constant oxygen partial pressures, increased the desulfurization rate, but enrichment to 0.33 atm caused the rate to decrease. At constant carbon dioxide partial pressures, the desulfurization rate was maximum at oxygen partial pressures of 0.21 and 0.30 atm. At higher (0.40 atm) and lower (0.14 atm) oxygen partial pressures the rate decreaed by 9 to 20%. The desulfurization rate decreased by 58X, from 9.0 to 3.8 mg S/1 hr, when the air pressure was increased from 1 atm to 3 atm. The effects justify an economic analysis during design and operation of a commercial air feed in a process to desulfurize coal by microbial action.

Jan 1, 1986

By J. P. Ulery

As a result of several recent methane/dust ignitions in surface auger and highwall mines, the U.S. Bureau of Mines investigated the occurrence of methane gas at these operations. Three mine sites were visited in western Kentucky and one in western Pennsylvania to collect run-of-mine coal samples for gas content determination using the modified-direct-method (MOM). Results indicate the samples emitted small quantities of methane, carbon dioxide, and nitrogen. Either methane or nitrogen was the predominant gas released. The same gases were released after crushing the samples for residual gas content; however, nitrogen was the primary component of this fraction. Total ~as contents ranged from less than 0.01 cm /g to 0.54 cm3/g. The hydrocarbon gases probably originated during coalification. Other gases may have originated partially as a byproduct of coalification and partially as a result of other, near-surface processes. The data suggest that although methane quantities are small, desorption could occur at near surface conditions prior to mining. The desorbed methane could accumulate as a free gas in fractures in the coal bed or roof rock. When these fractures are penetrated by the auger, methane could rapidly enter the whole atmosphere possibly creating explosive conditions.

Jan 1, 1994

By Manuel Gutierrez, Roberto Gomez, Juan Aravena, Johan Gjoevad

The use of explosives in mining operations is a process that involves the search for an ideal explosive for the type of geological condition of the mineral to be extracted. For the explosives present on the market the majority are based on Ammonium Nitrate. This as it is an ideal balance of high energy efficiency achieved with low development of gas emission. The manufacturing and loading operation of the explosive requires multiple process stages and different raw materials, which, if is not correctly supervised and controlled may cause the development of harmful gases or, in the worst case, even toxic gases. The majority of mining operations are located at remote locations without the presence of communities, and hence individuals, which could be affected by emission of the harmful or even toxic gases. In these operations the protection is mainly to protect the employees of the operation. However, if the operation is located near communities, the effect of these gases becomes a serious problem. The communities' perception of post-blasting gases, according to interviews carried out in this project, describes these as smells of black gunpowder, damp soil with a volatile permanence and medium intensity, sometimes a stinking tone is added. The legislation in Chile that controls the exposure of “workers” to different gases is Supreme Decree 594, 2019 (Decreto Supremo 594). Currently the Chilean Ministry of Environment and Sernageomin (Servicio Nacional de Geología y Minería) are taking actions to reform and strengthen oversight, seeking through a short law to provide more tools to the government to decentralize decisions in case of non-compliance with the decree. This paper describes the development and implementation of a permanent and remote gas monitoring system, considering the reasons for choosing the gases to be included in the equipment, the types of sensors and their capabilities, the way to verify in the field the correct functioning of the technology throughout the project, and finally how the data collected in the field is meeting the government's expectations in terms of permanent and online reportability. Additionally, it addresses the continuity of gas monitoring in the community that will disappear in the short term due to the expansion of mining operations, thereby ensuring the protection of both workers and affected communities.

Jan 21, 2025

By Z. Xie

Gas diffusion electrodes (GDEs) for high temperature polymer electrolyte fuel cells (PEFCs) have been prepared using ZrP-modified Nafion ionomer. The performances of these GDEs as cathodes and anodes were evaluated and compared with conventional Nafion ionomer GDEs using Nafion 112 as the PEM under elevated temperature and reduced relative humidity. ZrP-modified Nafion ionomer was incorporated into the catalyst layer to enhance water retention and/or increase the protonic conductivity. The fabrication of ZrP-GDEs was implemented by the ion exchange of Nafion solution with zirconyl chloride, followed by the impregnation of GDEs in H3PO4 solution. The composite electrolytes in the catalyst layer possessed a ZrP content of 20% by weight. GDEs were characterized by TGA, SEM, XRD, and CV. Scanning electron microscopy (SEM) indicated evenly distributed elemental Zr and P within the catalyst layer. Cyclic voltammetry shows a reduced electrochemically-active surface area when the ZrP is incorporated into GDEs. Polarization and impedance analyses indicate the cathode with ZrP-modified Nafion ionomer did not show an enhanced or decreased performance, compared with conventional Nafion ionomer GDEs under elevated temperature and decreased humidity. However, when GDEs with ZrP¬Nafion ionomer were used as the anode, an improved performance was observed. Preliminary experiments show that the anode is more sensitive to dehydration than the cathode under elevated temperature and/or low humidity. Improving the anode water retention capability will help to reduce losses at the anode. However, the incorporation of hygroscopic agents in the cathode catalyst layer is not essential because it is self-humidified by electrochemically-produced water even under elevated operating temperature and lower humidity.

Jan 1, 2005

By Baisheng Nie

The process of gas diffusion through coal particles and the mathematical physical model under the third kind boundary condition was determined to obtain the rules of gas diffusion through coal particles of different sizes. The analytical solution of the equation was obtained by the Method of Mathematical Physics. The parameters of analytical solutions and the implications of parameters were analyzed. The Biot criterion (Bi) and the Fourier criterion (F0) of mass transfer can represent and reflect the features of gas diffusion field of coal particles. Moreover, the measurement method of gas diffusion coefficient and surface mass transfer coefficient is introduced and an example of measurement is given. The achievement can provide the support to prevent disasters related to methane in coal mines.

Aug 1, 2013

By Das A. K

Investigations were carried out to understand the effect of liquid viscosity (u = 1 x 10-3 - 5 x 10-&apos; Ns/m2) on the size of primary bubbles formed at high gas injection rates (Q = 100 - 1000 cc/s, U = 0.04 - 0.42 mach) under room temperature conditions using flush tuyere (3 mm diameter) operating vertically upward. Tuyere pressure fluctuations were correlated to the mode of bubble formation by simultaneously filming the bubble and the corresponding tuyere pressure fluctuations displayed on an oscilloscope screen. A simple mathematical treatment is presented to estimate bubble size in viscous liquids. The theoretical results are compared with the experimental measurements.

Jan 1, 1987

Mixers are commonly used for the transfer of oxygen in gas-liquid-solid reactions in minerals processing. The process rate is usually controlled by two steps: gas-liquid mass transfer and reaction kinetics. Some examples are described along with the factors used for analysis of the mass transfer design problem. Typical oxygen rates and appropriate types of aeration systems or mixers are reviewed. The commonly used Rushton turbine has limitations in a number of mineral processes. The development and characteristics of the LIGHTNIN A315 axial flow gas dispersion impeller are described. Some practical examples which highlight its advantages are briefly described.

Jan 1, 1992

By Cesar Gomez, Jaime Álvarez, Lisette Wen

Laboratory mechanical flotation cells are extensively used in mineral processing for running batch flotation tests with a variety of purposes, for example assessing feed characteristics, determining flotation kinetics, or testing of new reagents and procedures. It is known that the results obtained depend on the operation mode, self-aerated or forced-air, and on the operating conditions selected for the test, in particular impeller speed and gas flow rate. These different results are a consequence of changes in size distribution of the generated bubble population and its remarkable evolution when frother is added; variations in bubble size affect the bubble surface area flux (BSAF), a variable which correlates with particle collection. Results of a two-phase (air-water) test program designed to measure bubble size for a variety of combinations of impeller type and speed, gas flow rate, frother type and concentration, and cell volume, demonstrated the wide range of BSAF with which the cell can be operated. The results obtained in this work demonstrated that gas dispersion in a forced-air lab flotation machine is significantly affected by the characteristics of the impeller/cell geometry combination in use, and the operating conditions selected. Operating conditions must be carefully selected and maintained during the test to ensure consistent results, in particular when frother concentrations below 20 ppm are used, because frother concentration in the cell will decrease as flotation progresses as a consequence of frother partitioning to the concentrate.

Jan 1, 2014

By Finch. J. A., C. Perez, J. M. Ortiz, G. Cortes, A. B. Yañiez, F. Coddou, P. Morales, H. Elgueta

A campaign to perform characterization tests in a TankCell®-300 flotation cell installed at Chuquicamata Codelco&apos;s concentrator was conducted. The campaign included integrated gas dispersion measurements (gas velocity radial mapping and single point gas holdup and bubble size) and determination of frother concentration. Cell streams were sampled to assess metallurgical performance at the same time. The experimental program was designed to establish the bubble surface area flux operating range and its effect on performance, and the effect of using longer residence times and of a device designed to enhance mixing in the collection zone (FlowBooster(TM)). The gas dispersion results and their relationship to metallurgical performance are discussed.

Jan 1, 2009

The effect of superficial gas rate distribution (Jg profile) on down-the-bank metallurgical response was tested in the rougher-scavenger bank (eight 10-m3 tank cells, 4 roughers and 4 scavengers) at Highland Valley Copper Mine&apos;s Cu/Mo separation circuit. Three Jg profiles were tested: (a) as found (i.e., typical practice), (b) increasing decreasing (i.e., increasing from cell 1 to 4 and decreasing from cell 5 to 8), and (c) decreasing-increasing (i.e., decreasing from cell 1 to 4 and increasing from cell 5 to 8). The Jg profile approach proved to be of considerable value. Profile (b) gave the best metallurgical results, i.e., the highest down-the-bank grade/recovery (increase in grade at constant recovery was approx. 3-4% compared to the as found case) and the most efficient Cu/Mo separation (cumulative Cu recovery was reduced by almost half - approx. from 20% to 12%, at 99% Mo recovery). The success of the evaluation prompted the implementation of profile (b). Detailed gas dispersion characterization tests (Jg and Db (bubble size)) showed significant discrepancies between the Jg measured directly (using the McGill University sensor) and the Jg calculated from field instrument readings (volumetric gas flowmeter) and machine dimensions (cell cross-sectional area). Tests were designed to reveal the source of disagreement. It was observed that a significant number of bubbles were not able to float (i.e., they were entrained with the tailings), the evidence appearing to be a significant number of very small bubbles (approx. 200-300 µm) which did not have sufficient buoyancy to rise. Consequently, rather than relying on the field instrument, the evaluation depended on the McGill University Jg sensor, which collects bubbles in a tube near the pulp-froth interface, thus providing significance to the data as the measurements were obtained from bubbles that almost certainly floated.

Jan 1, 2007

By J. A. Finch

"Gas dispersion in flotation defines the efficiency of the process once the chemistry has been established. There are three measurements, superficial gas velocity, gas holdup, and bubble size, which along with the derived quantity bubble surface area flux, are used to define “gas dispersion.” Sensors for measuring gas dispersion in industrial machines have been developed. This communication describes the working principle of the techniques and illustrates their potential to detect problems and to improve the operation of individual cells, banks and circuits. IntroductionFlotation is the most widely used process to separate minerals and is finding increasing application in other chemical and environmental fields. The process exploits natural and induced hydrophobicity to collect selected particles on the surface of a bubble. Once the process chemistry to control hydrophobicity has been established, the efficiency depends on dispersion of air to generate the necessary bubble surface area. Bubble surface area flux, Sb, the interfacial area generated per unit time and unit area of the machine, is emerging as one of the most useful variables to quantify gas dispersion (Gorain et al., 1997, 1998) although not without its critics (Heiskenan et al., 2001).For a bubble population of mean size db at a superficial gas velocity (or rate) Jg, the bubble surface area flux can be derived from geometric considerations (Finch et al., 1999):"

Jan 1, 2002

By D Alexander

For nearly 100 years, the flotation plant metallurgist has often wondered what is happening æbeneath the frothÆ. To assist in unravelling this mystery, new technology has been developed as part of the Australian Mineral Industries Research Association (AMIRA) P9 project, to measure gas dispersion characteristics (such as gas hold-up, superficial gas velocity and bubble size) in industrial flotation cells. These measurements have been conducted in a large number of cells of different types and sizes by researchers from the Julius Kruttschnitt Mineral Research Centre (JKMRC) and JKTech. A large database has been developed and the contents of this database are described in this paper. Typical cell characterisation measurements show a wide spread in values, even in the same cell types and sizes performing similar duties. In conventional flotation cells, the typical gas hold-up values range from 3 - 20 per cent, bubble sizes range between 1 and 2 mm, and superficial gas velocity ranges from 1 to 2.5 cm/s. The ranges of cell characterisation measurements given in this paper will enable plant personnel to compare their operation to other similar types of operations from around Australia and the rest of the world, giving opportunities for further improvement to flotation plant operations.

Jan 1, 2005

By Alejandro Yañez, Martta Nousiainen, Rodrigo Grau

"Gas dispersion plays a fundamental role in froth flotation. Gas dispersion in flotation is quantified by using four properties: gas velocity, bubble size, gas hold-up and bubble surface area flux. Gas dispersion measurements were conducted in three flotation cells: TankCell 1, TankCell e300 and TankCell e500. The measurements reported in this paper were carried out exclusively in two-phase systems using only water and air at frother dosages exceeding the Critical Coalescence Concentration (CCC) in order to prevent bubbles from coalescing. The measurements conducted in TankCell 1 and TankCell e500 were conducted by Outotec specialists, whereas the characterization of TankCell e300 had been conducted earlier in 2008 by a team from McGill University. When working in two-phase systems and under non-coalescing conditions, gas dispersion characteristics measured in different scales can be compared directly. The measurements conducted in TankCell e300 are taken as a base line in order to compare the performance of TankCell e500, whereas TankCell 1 is a pilot-scale flotation cell which is used in rotor testing. The gas dispersion properties in TankCells were found to be affected by the air flow rate and rotor tip speed. Bubble sizes (d32) measured on the three-size scale seem to be within the same range of 0.6 mm to 1.6 mm. It was noted that the bubble size was influenced by rotor tip speed and gas velocity. In general, as the rotor tip speed increased, the bubble size decreased and as the gas velocity increased, so did the bubble size. The rotor tip speed also has an impact on the hold-up; in general, as the rotor tip speed increased the gas hold-up also increased but the influence of air flow rate on gas hold-up was greater. Bubble surface area flux was found to vary between 40 and 85 1/s. As the gas velocity increased, the bubble surface area flux also increased."

Jan 1, 2014

By Avishan Atrafi, Marek Pawlik

"Gas dispersion properties of sodium salts of 6, 12 and 18-carbon fatty acids (hexanoic, lauric and oleic acid) were investigated as a function of pH. A strong effect of pH was observed on gas dispersion properties of fatty acids. At high pH for 12 and 18 carbon fatty acids, at which these surfactants formed a true solution, the gas dispersion properties were similar to those of MIBC. In the case of sodium hexanoate, which has a much higher solubility than the longer chain fatty acids and therefore does not form precipitates, the gas dispersion properties of this surfactant were strongly enhanced in the acidic pH range, where hexanoic acid was fully associated. This result is an indication that undissociated hexanoic acid is much more surface-active than anionic hexanoate. Only a small effect of the surfactant chain length on gas dispersion properties of the tested reagents was observed. The measured critical coalescence concentration (CCC95) values increase slightly by decreasing chain length and range from 5.8 x 10-5 mol/L (17.7 mg/L) for sodium oleate to 7.2 x 10-5 mol/L (16 mg/L) for sodium laurate at pH 10 and 1.9 x 10-4 mol/L (26 mg/L) for sodium hexanoate at pH 3.7. These are compared to CCC95 of MIBC, which is measured to be 8 x 10-5 mol/L (8 mg/L). The soluble molecular species were recognized as the most effective species in preventing bubble coalescence."

Jan 1, 2014