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By Charles Becker

THE practice of drying phosphate in Florida is as old as the industry, which began a little more than half a century ago. The methods, however, have changed considerably. At first, the natural process of exposure to the sun and air was used, later supplemented by wood fires beneath open-air stationary dry kilns and drying towers of various designs. It was not until the early nineties that rotary driers came into use, and at first they were of very small design and fired with wood. As the industry grew and tonnage increased, so likewise grew the number and size of rotary driers, until today the largest installations are 6 ft. up to 7 ft. 6 in. in diameter, and 55 to 60 ft. long, fired with crude oil. The reasons for drying phosphate rock are: (1) to eliminate freight on water in the shipment and (2) to facilitate the good grinding qualities required by the buyers in their acidulation. Phosphate pebbles vary materially in natural characteristics and each property has a direct bearing on the processing. In making comparisons of cost and operating conditions, the following are usually taken into consideration: 1. The hard dense pebbles, which contain very little interior moisture and 6 to 8 per cent total moisture, usually produced from the low-grade deposits. 2. The lighter, porous pebbles, which contain 4 to 5 per cent interior moisture and a total moisture ranging from 9 to 15 per cent. 3. The product of recovery operations using oily reagents, containing from 15 to 25 per cent moisture. 4. The size of the pebbles. Usually the plus 5-mesh material is considered as "coarse rock"; the minus 5-mesh plus 24-mesh is "fine rock," and the minute particles below 24 mesh are called "concentrate." 5. The amount of moisture allowed in the dried product. The practice is generally to dry down to 1.5 to 2 per cent moisture. There is, however, an actual range in guarantee of from 1 per cent maximum to 3 per cent maximum.

Jan 1, 1936

ZINC concentrate, produced at Zeehan by flotation from Read Rosebery ore, is also dried and roasted at the same place for the production of a calcine suitable for use in the electrolytic zinc process at Risdon, Tasmania.DRYINGThe concentrate, dewatered to 12% moisture by an American filter, is fed into a dryer, the type of construction of which is similar to that of a duplex Edwards furnace. The dryer is 45 ft. long and 14 ft. wide, and has two rows of nine rabbles each, the two pairs nearest the firebox being watercooled.The longitudinal distance between rabble-centres is 4 ft. The rabbles are rotated at a speed of 3 r.p.m. by a I5-h.p. motor. Zinc concentrate is introduced by a screw feeder, consisting of two parallel-blade conveyors, revolving in opposite directions at aspeed of 31 r.p.m.Draft is supplied by a Sirocco fan, 15 in. intake, operated at 1340 r.p.m. by a 10-h.p. motor. The dust carried by the exit gases is removed in a wooden scrubbing tower, 3 ft. 6 in. x 4 ft. 6 in. x 27 ft. high, to which the fan delivers, and down which water issprayed.Wood (eucalyptus timber) is used as fuel, the consumption per ton of water evaporated being 0.55 :ton. Zinc concentrate from the dryer passed either to trucks for shipment or to Herreshoff furnaces. The portion for shipment is withdrawn at a point half-way down the furnace, being loaded on to a belt conveyor for transfer to railway trucks. The moisture at this point is 7% to 8%.

Jan 1, 1927

By Abdellah Chlk, Driss Msatef

Sedimentary phosphate ores are known for their relatively high specific surface area and porosity, which have a positive influence on their reactivity when used as fertilizer in acidic soils or in the manufacture of wet phosphoric acid and phosphatic fertilizers. However, these physical properties could have a negative effect on the behavior of these ores if dried. This effect has been studied on several phosphate ores samples by: the determination of mineralogical and textural properties of these samples, the determination of vapor water sorption isotherms, at different temperatures, from which the sorption heat has been calculated, carrying out several drying tests using a laboratory fluidized bed reactor under constant conditions, which showed important differences in drying rates and residual moistures.

Jan 1, 1999

By E. O. Wagner, V. F. Parry

This paper summarizes investigations during 1949 on three pilot plants for drying low-rank fine coal by entrainment in hot gases. Detailed operating results on processing seven coals having moisture ranging from 24 to 62 pct, formulas and data for calculating performance of large units, and general conclusions on the problem of drying fine coal are presented.

Jan 9, 1950

By Beeby C. j, Fernando W. J, Ming M. Q I, Guang Li Xi

Removal of moisture in steam-fluidized, mainly steam-heated, fluidized beds makes possible significant energy savings over conventional forms of large-scale drying. The systens are described and their applications to brown coal and alumina hydrate are reviewed. In application to brown coal the use of the system to permit meeting diurnal variation in power station output, and the use of triple-effect drying to minimise coal usage and to avoid the necessity of recovering in the turbines the energy in the steam from the last dryer are discussed. To facilitate the rapid adoption of the systems proposed, studies are being made of heat-transfer to dried coal, of moisture equilibrium in pressurized and vacuum systems, of tapered beds as a means of reducing carrier steam and permitting wider size variation, and of the use of carrier solids for drying lump materials.

Jan 1, 1989

By V. F. Parry, J. B. Goodman

The low-rank coals containing 10 to 50 pet natural bed moisture represent over half of the tonnage reserve of the available solid fuels of the United States, but only about 2 pet of United States coal production is derived from these fuels. Increased utilization of these large reserves will result if the bed moisture can be removed at the mine in high-speed low-cost processes. This paper presents a theoretical and experimental study of the factors affecting high-speed drying of coal dusts. The time required to heat particles of coal is proportional to the square of their diameter, and it is calculated that the probable time in minutes is equal to 6D2. In other words, a 11 a in. coal particle should be heated to drying temperature in 1.5 to 2.0 sec. Likewise, 1/8 in. particles should be heated in about 6 sec. The net heat required to dry subbituminous coal and lignite varies from 240 to 375 Btu per pound, depending upon the moisture removed, and this heat can be obtained from 42 to 61 cu ft of hot gases at 600°F.

Jan 1, 1949

By E. O. Wagner, V. F. Parry

This paper summarizes investigations during 1949 on three pilot plants for drying low-rank fine cool by entrainment in hot gases. Detailed operating results on processing seven coals having moisture ranging from 24 to 62 pct, formulas and data for calculating performance of large units, and general conclusions on the problem of drying fine coal are presented.

Jan 1, 1950

By V. F. Parry, E. O. Wagner

This paper summarizes investigations during 1949 on three pilot plants for drying low-rank fine coal by entrapment in hot gases. Detailed operating results on processing seven coals having moisture ranging from 24 to 62 pet, formulas and data for calculating performance of large units, and general conclusions on the problem of drying fine coal are presented. THIS paper presents a summary of investigations by the Coal Branch of the Bureau of Mines during 1949 on the removal of internal moisture from low-rank coals by processing them in the entrained and fluidized state. A paper on this subject, giving a summary of the early work, was presented at the 1949 AIME annual meeting1 and gave a the- oretical discussion of the time and heat required to dry various sizes of low-rank coal. The investigations on two pilot plants were presented in the foregoing paper. During 1949, three additional pilot plants were built to study phases of the drying problem and to investigate different techniques of handling fine coal in the entrained and fluidized state. The present paper gives operating data on the new units and presents detailed data on the drying of seven coals having bed moisture ranging from 62 to 24 pct. The problem of removing surface moisture from fine coal is principally one of heat exchange and dispersion of the coal particles so that heat can reach the liquid moisture to permit evaporation, and it does not involve the factors of size and time of contact to any great extent. If enough heat can reach the surface of the particles at temperatures higher than 250°F, moisture evaporates almost instantly, and the factors of time and size are of secondary importance compared with the factors of heat balance and dispersion of the coal. Therefore, it does not appear to be necessary to employ a fluidized bed when removing surface moisture, and the most efficient process would be one in which the coal particles are entrained in a hot gas stream of optimum temperature traveling at a velocity that causes the particles to disperse into a low-density phase. When low-rank coals are dried, the fluidized bed is necessary to provide control of time of contact. This is done by adjusting the superficial velocity which controls the density or dispersion of the particles. The density of beds having fluidized properties suitable for drying low-rank coals appears to range from about 5 up to about 15 lb per cu ft. When the density is below 5 lb per cu ft, which represents a low-density phase, optimum conditions for removal of surface moisture should be found, and this requires superficial velocities of about 15 fps. The problem of removing bed moisture from low-rank coals involves consideration of size of coal, temperature, mass flow, heat balance, pressure, time of contact, and method of dispersing the coal in the heating mediums. The experimental work presented here gives data on these factors. Coal sizes up to 1/2 in. x 0 were dried with hot gases having initial temperatures ranging from 1900° to 2400°F. Coal

Jan 1, 1951

By E. O. Wagner, V. F. Parry

This paper summarizes investigations during 1949 on three pilot plants for drying low-rank fine coal by entrapment in hot gases. Detailed operating results on processing seven coals having moisture ranging from 24 to 62 pet, formulas and data for calculating performance of large units, and general conclusions on the problem of drying fine coal are presented. THIS paper presents a summary of investigations by the Coal Branch of the Bureau of Mines during 1949 on the removal of internal moisture from low-rank coals by processing them in the entrained and fluidized state. A paper on this subject, giving a summary of the early work, was presented at the 1949 AIME annual meeting1 and gave a the- oretical discussion of the time and heat required to dry various sizes of low-rank coal. The investigations on two pilot plants were presented in the foregoing paper. During 1949, three additional pilot plants were built to study phases of the drying problem and to investigate different techniques of handling fine coal in the entrained and fluidized state. The present paper gives operating data on the new units and presents detailed data on the drying of seven coals having bed moisture ranging from 62 to 24 pct. The problem of removing surface moisture from fine coal is principally one of heat exchange and dispersion of the coal particles so that heat can reach the liquid moisture to permit evaporation, and it does not involve the factors of size and time of contact to any great extent. If enough heat can reach the surface of the particles at temperatures higher than 250°F, moisture evaporates almost instantly, and the factors of time and size are of secondary importance compared with the factors of heat balance and dispersion of the coal. Therefore, it does not appear to be necessary to employ a fluidized bed when removing surface moisture, and the most efficient process would be one in which the coal particles are entrained in a hot gas stream of optimum temperature traveling at a velocity that causes the particles to disperse into a low-density phase. When low-rank coals are dried, the fluidized bed is necessary to provide control of time of contact. This is done by adjusting the superficial velocity which controls the density or dispersion of the particles. The density of beds having fluidized properties suitable for drying low-rank coals appears to range from about 5 up to about 15 lb per cu ft. When the density is below 5 lb per cu ft, which represents a low-density phase, optimum conditions for removal of surface moisture should be found, and this requires superficial velocities of about 15 fps. The problem of removing bed moisture from low-rank coals involves consideration of size of coal, temperature, mass flow, heat balance, pressure, time of contact, and method of dispersing the coal in the heating mediums. The experimental work presented here gives data on these factors. Coal sizes up to 1/2 in. x 0 were dried with hot gases having initial temperatures ranging from 1900° to 2400°F. Coal

Jan 1, 1951

By Marco Le Roux, Martha Van Rensburg, Quentin Campbell

Fluidised bed drying is currently receiving much attention as a dewatering option during the beneficiation of fine (defined here as between 1 mm and 2 mm particles) coal. Apart from concerns about safety and combustion, the operating costs can be high if very high gas or air temperatures are used. The aim of this study was to investigate the removal of moisture from fine coal by using air at a lower temperature (25 - 55°C) within a controlled environment by lowering of the relative humidity of the air. It was firstly proven that fluidization has a major advantage over non-fluidized beds, with regards to drying rate and final moisture content. Hereafter several parameters that influence the dewatering rate and final moisture content were tested, from which it was concluded that the relative humidity of air acts as the largest driving force for dewatering. Parameters tested included relative humidity, temperature and coal composition. Energy balances showed a positive nett energy increase in the dried coal during combustion when related to the energy input during drying. In comparison with thermal drying technologies, fluidized bed drying was proven to be less energy intensive. It was therefore shown that this is a viable technology for the dewatering of fine coal.

Jan 1, 2014

By T Muri

The drying operation of materials from particulate solids, through slurries and suspensions, to continuous sheets represents an important part of several processes in the chemical and mineral industries. The increasing demand of high productivity at low cost and minimal environmental impact makes it complex to evaluate and choose the best available drying technology for each industrial application. The drying technologies are mainly characterised on the basis of how the wet product is related to the drying medium, namely: direct and indirect drying. In the direct drying method (convection drying), the product is brought into direct contact with the drying medium, which may be hot gas or air. Large quantities of gas are necessary for transfer of the required energy. A special case of the direct dryer is the fluid bed dryer, in which the product floats on a cushion of air or gas. The process air is supplied to the bed through a perforated distributor plate and flows through the bed of solids at a velocity sufficient to support the weight of particles. Very high heat and mass transfer values are obtained as a result of the intimate contact with the solids and the relative velocities between individual particles and the fluidising gas. In the indirect drying method (conduction or contact drying), the wet product is separated from the drying medium. The drying unit can consist of a rotor forming the indirect contact heating surface mounted in a stationary or rotating shell. The indirect method uses saturated or superheated steam resulting in low energy consumption and minimal environmental impact. In this paper, a review is given of the technologies available on the market based on different drying methods. The advantages and the disadvantages are summarised with respect to issues such as investment and operating cost, maintenance, product capacity, product handling and environmental impact.

Jan 1, 2006

By J. Pinkley

DSI DYWI Rock Dust application is aiding in enhancing safety and productivity in underground coal mining. DSI DYWI Rock Dust combines wet dusting technology and polymers to allow for drying and lift characteristics for rock dusting. DSI DYWI Rock Dust typically dries within 24 to 48 hours depending upon the mine air velocity and humidity. The DSI DYWI Rock Dust Applicator Machine is a completely hydraulic unit. The DSI DYWI Rock Dust Applicator machine allows for batching of product and face spraying operations in permissible locations. The DSI DYWI Rock Dusting Applicator Machine fits in one half of a battery or diesel scoop bucket for ease of transport. It is completely hydraulically powered by the PTO circuit. The DSI DYWI Rock Dust Applicator unit requires a scoop operator, and a person to operate the spray wand, simple operation with two personnel. The first demonstration was at an underground continuous miner room and pillar coal mine which produced a pilot test period opportunity, which proved to be successful, and has now been in full launch mode with the US underground coal mining industry. A typical batch of operation allows for 250? of roof and rib (19? wide by 6? in height) coverage of DSI DYWI Rock Dust application. The DSI DYWI Rock Dust Applicator contains a hydraulic powered air compressor which allows for 30-50% more coverage per batch by improved dispersion of product via air assist spray nozzle. DSI DYWI Rock Dust will add approximately $0.02 to $0.04 per clean ton of coal cost to the mining operation over traditional rock dust cost depending upon mining height.

Jan 1, 2012

By Maria Thornhill, Rolf Arne Kleiv

INTRODUCTION The last decade has given rise to an increasing number of deep-sea mining concepts (DSMCs) outlining technical solutions for the production chain from seafloor mining to mineral or metal extraction. The vast technological and logistical challenges coupled with immature but rapidly evolving technology has spawned a great variety in proposed concepts, and the exact implications of the phrase ‘best available technology’ is very much an open question. DSMCs differ significantly with respect to choice of technology, technological readiness level, degree of resource utilization, logistics, OPEX and CAPEX requirements, overall profitability, legal and political implications, not to mention environmental impact. Hence, a system for classifying concepts could provide a useful identification and structuring tool when performing economic, judicial or environmental assessments of DSMCs, as well as offering a general terminology to describe concepts sharing fundamental traits. This abstract proposes a DSMC classification system based on how a concept makes use of mineral separation at the different stages in the ore’s journey from the deposit to the ocean surface and ultimately to onshore facilities. Mineral separation, as a process step, is the key factor in determining both the state and mass flow of materials along the production chain and has, as such, a decisive effect on economy and environmental impact of any deep-sea mining project. A DSMC that is based on bringing the entire volume of broken ore to onshore facilities for processing will look very different from a concept based on pre-concentration (i.e. mineral separation) at the seafloor. Whereas the latter offers savings in the form of reduced energy cost for vertical transport, it also represents a substantial additional technological challenge. Furthermore, whether or not a concept relies on mineral processing at the seafloor or on a floating facility at the ocean surface above the deposit also determines the point at which mineral separation waste (i.e. tailings) must be managed. Different concepts offer different opportunities for tailings deposition, and are at the same time bound by different requirements.

Jan 1, 2018

By Leon Keller, William R. Van Slyke, James Stukel

Two 4-ft wide DSM screens were installed during 1957 in one unit of the two-unit heavy media cy- clone section of the Holman-Cliffs concentrator at Taconite, Minn., following successful laboratory test work on a 1-ft screen. The two screens materially reduced the amount of media sent to the magnetic separator cleaning circuit. Wear life was good and fine size capacity was high. Briefly, the Holman-Cliffs heavy media cyclone plant uses -65 mesh magnetite as media and 10-in. diam., 30º Ni-Hard cyclones as separatory vessels. Feed to the plant averages 130 long tons per hr of -1/8 in. +65 mesh material. The conventional heavy media circuit uses drum or spiral type separatory units and treats +l/8 or 3/16-in. material. The medium is generally -65 mesh ferrosilicon. Ore and media are readily separated by screening at about 6 mesh. At this size, capacity is high and wear and maintenance are not excessive. The heavy media cyclone plant requires an efficient separation between +65 mesh ore and -65 mesh media. To reduce costs, however, the separation was made at a coarser size with the result that the media was un- duly contaminated and it was necessary to clean large tonnages of media and ore in magnetic separators. Due to the high capital cost of these units, their number was kept to a minimum and, consequently, they were overloaded. As a result, the separation between magnetic media and nonmagnetics was not sharp and the magnetite losses were high.

Jan 10, 1958

By Remo Grandori

"INTRODUCTIONDouble Shield TBMs were introduced in the market in the early seventies with three main targets:• Increase the TBM performances in term of advance per day thanks to the ability to erect a segmental lining simultaneously with the excavation phase.• Be able to advance through unstable and disturbed rocks under the protection of the shields• Provide a finished tunnel by installing a precast lining as the TBM advance.In 2003 SELI developed the design of the Double Shield Universal (DSU) TBM as an evolution of the original Double Shield TBM design.This new TBM design was targeted to improve: the TBM capability to advance through squeezing/converging rock formations under high cover, the telescopic joint design (allowing by such to operate the machine in double shield mode in very weak rock), the capability of the TBM to investigate and treat the ground around and ahead of the tunnel face.In the same lapse of time Single Shield TBMs, originally utilized for soft ground tunnelling, extended progressively their range of application to mix rocks and finally to hard rock tunnelling with increasing performances.This also thanks to the substantial reduction in the installation time of the segmental lining ring that contributed to minimize the TBM stand by time between two consecutive boring strokes.Today the choice between the two types of TBMs needs to be carefully evaluated project by project since one type of TBM may “prevail” in certain geologies and diameters and vice versa.THE VISHNUGAD PIPALKOTI TUNNELThe Vishnugad Pipalkoti Tunnel is part of the 444 MW Vishnugad Pipalkoti Hydro Electric Project (VPHEP) on Alaknanda river in Uttarakhand (India).The Owner is the Indian electric company “Tehry Hydro Development Corporation” (THDC) and the World Bank finances the project.The Headrace Tunnel total length is 13.4 Km and a section of about 12,3km will be excavated by TBM by SELI Overseas (Italy) in subcontract to HCC (India) the General Contractor for the project. The TBM will be delivered ex workshop in March 2016 and it is foreseen to start boring in the second half of 2016.Figure 1 below shows the location of the project and the following Table 1 summarizes the geometrical characteristics of the TBM tunnel."

Jan 1, 2016

By F. Hassan, M. A. Arafa

At El-Gedida iron ore deposits there is a block of about 30million tons neglected due to its higher sulfur content due to the presence of barite gangue minerals. From this bluk by magnetic separation dual concentrates of high grade iron concentrate (~65%Fe and total Sulfur of 0.26%) and the second concentrate is barite of (60.87% BaO and total impurities of less than 3%).

Jan 1, 1999

By John T. Watson, Jim Bailey

Increasing public awareness is probably the single most important challenge faced by any blasting contractor today. This increased awareness usually results in an outcry for tighter regulations and restrictions on those in the blasting industry. Those affected do not often understand the dynamics of blasting and are simply fearful of the unknown. This reaction very often results in more regulations and restrictions which frequently fail to address the real problems.

Jan 1, 1990

By H. U. R. Kattentidt, W. L. Dalmijn, T. P. R. de Jong

"Research at Delft University aims to develop systems for automatic inspection and sorting of bulk solids which can be applied in the mineral processing and recycling industry. A recent development includes an automatic sorter based on airport X-ray inspection technology. It is designed for continuous inspection and sorting of 5 - 150 mm solids and has as objective a cost effective and high capacity on-line inspection and sorting.Dual energy X-ray transmission imaging provides instantaneous data about particle dimensions and the atomic number distribution. The system provides particle thickness and average atomic number on a pixel level at scanning speeds between 250 and 500 lines / second. With existing X-ray components inspection speeds between 0.5 and 2 m/s at approximately 1-meter inspection width and between 1.5*1.5 and 5*5 mm2 sensor resolution can be achieved.Imaging algorithms that were developed by Delft University for applications in recycling, waste cleaning and other applications acquire shape, size distribution and composition data. Currently on-line processing of a product at a rate of around 200 particles per second is possible using a standard PC. Experiments with a demonstration X-ray unit indicated good potential for various applications in solids processing. They include continuous inspection of organic content, sulphur, chlorine, ash, and metal distribution. It is applicable for coal cleaning, ore sorting, industrial minerals, and various applications within waste cleaning and recycling. Dual energy X-ray transmission fundamentals and recent progress in system development and applications are presented."

Jan 1, 2003

By H. U. R. Kattentidt, W. L. Dalmijn, T. P. R. de Jong

"Research at Delft University aims to develop systems for automatic inspection and sorting of bulk solids which can be applied in the mineral processing and recycling industry. A recent development includes an automatic sorter based on airport X-ray inspection technology. It is designed for continuous inspection and sorting of 5 – 150 mm solids and has as objective a cost effective and high capacity on-line inspection and sorting.Dual energy X-ray transmission imaging provides instantaneous data about particle dimensions and the atomic number distribution. The system provides particle thickness and average atomic number on a pixel level at scanning speeds between 250 and 500 lines / second. With existing X-ray components inspection speeds between 0.5 and 2 m/s at approximately 1-meter inspection width and between 1.5*1.5 and 5*5 mm2 sensor resolution can be achieved.Imaging algorithms that were developed by Delft University for applications in recycling, waste cleaning and other applications acquire shape, size distribution and composition data. Currently on-line processing of a product at a rate of around 200 particles per second is possible using a standard PC. Experiments with a demonstration X-ray unit indicated good potential for various applications in solids processing. They include continuous inspection of organic content, sulphur, chlorine, ash, and metal distribution. It is applicable for coal cleaning, ore sorting, industrial minerals, and various applications within waste cleaning and recycling. Dual energy X-ray transmission fundamentals and recent progress in system development and applications are presented."

Jan 1, 2003

By T. P. R. de Jong

Dual energy X-ray transmission imaging is extensively applied for safety luggage inspection. Its advantages are its rapid scanning rate (25 to 100 cm/sec) at approximately I mm resolution and simultaneous thickness independent metal identification. This is especially advantageous for secondary scrap metal inspection and automatic sorting. Other applications include metal product inspection, bale control, and waste processing. Recent progress in development of an automatic on-line sorter for bulk solids is presented and discussed. Besides various non-metal applications (solid fuels, wastes etc.) it appeared particularly effective in light metal sorting. As inspection tool better control of difficult to monitor solid bulk streams, batteries, bales and other related metals becomes possible.

Jan 1, 2003