Rafstöðugreining á fosfati: Umfjöllun um fyrri störf og umræður um Óforskilna Aðskilnaðarkerfi

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Engineering kom 00 (2015) 000–000

www.elsevier.com/locate/procedia

3rd International Symposium um nýsköpun og tækni í fosfat iðnaður

Electrostatic beneficiation af fosfat ores: Endurskoðun á eldri vinnu

og umræðu um bætt aðskilnaðarkerfi

J ð ð ð ð ð. BittnerA, S.A.GasiorowskiA, F.J.HrachA, H. Guicherdb* ð

AST Equiment og tækni LLC, Needham, Massachusetts, Bandaríkin

BST Equipment & tækni LLC, Avignon, Frakkland

Óhlutbundnar

Beneficiation af fosfat ores með þurrum rafsegulferlum hefur verið reynt af ýmsum vísindamönnum frá því um 1940's. Undirliggjandi ástæður fyrir þróun þurrferlis fyrir fosfat bata eru takmarkað magn af vatni í sumum arid svæðum, á flotun efnakostnaðar, og meðferðarkostnaður wastewater. Þó rafsegulferlar mega ekki veita fullkomið val á flotun, það kann að henta sem viðbót fyrir suma strauma eins og að draga úr sektum / slimes efni ore áður en flotun, vinnslu flotun tailings fyrir endurheimt glataður vara, og lágmarka umhverfisáhrif. Þó að mikil vinna var framkvæmd með bæði hár spenna Roller og freefall skiljur á rannsóknarstofu vog, eina sönnun þess að auglýsing uppsetningu er circa 1940 "Johnson" ferli hjá Pierce Mine FL; Engar vísbendingar eru í bókmenntum um núverandi viðskiptalega notkun rafsegullyfja, þó sterkur áhugi á þurrum ferlum haldi áfram til notkunar á arid svæðum. Í ýmsum rannsóknarverkefnum var lögð áhersla á að fæða undirbúning (Hitastig, stærðarflokkun, ástand umboðsmanna) hafa mikil áhrif á frammistöðu. Þó nokkur góður aðskilnaður hafi náðst með því að fjarlægja kísil úr fosfór, og með færri dæmum um kalk og dolomite úr fosfati, niðurstöðurnar eru minna jákvæðar þegar margar hvatar eru til staðar. Rannsóknarvinna heldur áfram að betrumbæta þessar aðferðir, but fundamental limitations on the conventional electrostatic systems include low capacity, the need for multiple stages for adequate upgrading of ore, and operational problems caused by fines. Some of these limitations may be overcome by newer electrostatic processes including a triboelectric belt separator.

© 2015 The Authors. Published by Elsevier Ltd.

Peer-review under the responsibility of the Scientific Committee of SYMPHOS 2015.

Leitarorð: Fosfat, electrostatic; separation; Steinefni; fine particles; dry process

*Corresponding Author: Tel: +33-4-8912-0306 E-mail address: guicherdh@steqtech.com

1877-7058 © 2015 The Authors. Published by Elsevier Ltd.

Peer-review under responsibility of the Scientific Committee of SYMPHOS 2015.

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1. Reported work on electrostatic beneficiation of phosphate ores

Phosphate concentration from natural ores has long been performed by a variety of methods using sometimes substantial amounts of water. þó, due to the shortage of water at various phosphate deposits around the world, as well as increasing costs of permitting and wastewater treatment, the development of an effective, economic dry process is highly desirable.

Methods for dry electrostatic processing of phosphate ores have been proposed and demonstrated at small scales for over 70 Ára. þó, commercial applications of these methods have been very limited. The “Johnson process” [1] was used commercially starting in 1938 for a period of time at the American Agricultural Chemical Company plant near Pierce Florida USA. This process used a very complex series of roller electrodes (Mynd 1) for the multi stage concentration of phosphate recovery from deslimed washery tailings, flotation pre-concentrates, or flotation tailings. Starting with 15.4% P2O5 og 57.3% insoluble material in the fine tailings, through a combination of size classification, desliming, and preconditioning of the dried tailings, the material with 33.7% P2O5 and only 6.2% insoluble was recovered. In another example, upgrading of flotation tailings with 2.91% P2O5 resulted in a product of 26.7% P2O5 with an 80% recovery. Johnson observed that it was necessary to treat the washery tailings with chemical reagents typically used in phosphate flotation to obtain high phosphate grade and recovery. He specifically mentions the effectiveness of fuel oil and fatty acids as reagents.

Mynd 1, Johnson process apparatus and flow sheet US Patent 2,135,716 og 2,197,865, 1940 [1][2]

While this commercial installation is cited in the literature as starting about 1938, it is not clear how extensively or for how long this process was used. In his summary of the status of electrostatic separations up to 1961, O. C. Ralston

[3]writes that five large Johnson separators were installed each processing about 10 tons/hr of -20 mesh feed. Each separator was 10 rolls high with the applied voltage of 20 kV. No other commercial-scale phosphate concentrators using electrostatics were installed in Florida according to Ralston. Based on the process equipment description, the authors

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have concluded that the overall capacity of the process was rather low in relation to the capacity of other processes, such as wet flotation. Low capacity and the costs of drying the feed ore from wet mining in Florida are likely the reason for limiting the further application of the process in the 1940s and 1950s.

In the 1950’s and 1960’s workers for International Minerals & Chemicals Corporation (IMC) examined the application of dry electrostatic separation processes for mineral beneficiation. Floridian phosphate ore processing was of particular interest to IMC. The IMC work utilized a free fall separator design sometimes with particle charging enhanced by passing through an agitator or impactor such as a hammer or rod mill. [4] A subsequent patent [5] included some enhancement of the separation using chargers of different materials, though the final patent in the series

[6]concluded that particle contact charging at an elevated temperature (>70°F) was more effective than using a charger system. Representative examples of results reported in these patents are shown in Table 1.

Table 1. Reported results from International Minerals & Chemicals Patents 1955-1965

The various IMC patents examined the influence of particle size, including processing of various screen cuts independently, though little work involved very fine (<45 Μm) particles. Sample conditioning varied widely, including temperature adjustment, pre washing and drying, and different drying methods (indirect drying, flash drying, heat lamps with specific IR wavelength ranges). Different impurities (þ.e.. silicates versus carbonates) required different handling and pretreatment methods to optimize the separation. While it is clear from the patent descriptions that IMC was attempting to develop a commercial scale process, examination of the literature does not indicate that such an installation was ever constructed and operated at any IMC site.

In the 1960’s work specifically on carbonate containing phosphate ores from North Carolina was performed at the North Carolina State University Minerals Research Laboratory, [9] Using a laboratory scale freefall separator and a synthetic mixture of ground shell carbonate and phosphate pebble flotation concentrate in a very narrow size range (-20að +48 mesh), the research showed that preconditioning the material with an acid scrub or fatty acids influenced the relative charge of the phosphate as either positive or negative. Relatively sharp separations were obtained. þó, when using a natural ore containing a considerable amount of fines, only poor separations were possible. The best reported separation from a residue from flotation upgrading with an initial P2O5 concentration of 8.2% recovered a product of 22.1% P2O5. No recovery level was reported. Notably, one of the reported difficulties was a build-up of fines on the separator electrodes.

Additional work on electrostatic separation of North Carolina phosphate using a high tension roller type separator

[10]concluded that while the separation of phosphate and quartz was possible, drying cost was prohibitive. þó, given that calcined phosphate ores are dry, the researchers suggested that electrostatic separation of such ores may be possible. Separation of calcined phosphates was poor in the reported work. Separation appeared to be related to particle size rather than composition. Suggested improvements included the use of other electrostatic separation systems, reagents to enhance particle charging characteristics and very close screen sizing of materials. There is no evidence that any follow-up work was performed on this project.

Somewhat earlier work using high-tension roller separators [11] successfully removed aluminum and iron compounds from run-of-mine ore from Florida. The ore was dried, crushed, and carefully sized prior to separation. The P2O5 concentration was increased marginally from 30.1% að 30.6% but the removal of the Al and Fe compounds enabled a much better subsequent recovery by flotation methods. This work illustrated the use of an electrostatic separator to address a problem with a specific ore that limited conventional wet processing.

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Along with investigations into the separation of many other materials, Ciccu and co-workers tested the separation of a variety of phosphate ores including sources from India, Alsír, Túnis, and Angola. [12] Electrostatic separation was of interest as an alternative to flotation from an economic standpoint due to the fact that large deposits of phosphates are found in arid regions. [13] Using laboratory-scale free fall separators with a “turbocharger”, these researchers were able to obtain separation results similar to flotation processes from ores with relatively simple gangue compositions. Specifically, they found that phosphate charged positively in the presence of silica, but negative in the presence of calcite. þó, if the ore contained significant amounts of both silica and carbonate, the electrostatic separation was poor and flotation processes proved more flexible for obtaining practical separations. From studies of the effects of the turbocharger on charging of individual particles, these researchers concluded that the gangue material charged primarily by particle-particle contact rather than contact with the turbocharger surfaces. [13] [14] Charging was also highly sensitive to material temperature, with good separation only obtainable above 100°C. Additionally, the presence of fine material caused problems in the separator and good results depend on careful sizing of particles in up to three size ranges prior to separation. A summary of the results from this group is presented in Table 2. No full- scale applications appear to have been implemented based on this work.

Table 2. Reported results from Ciccu, et. al. from laboratory-scale free fall separators

Electrostatic separation of an Egyptian ore was studied by Hammoud, et al. using a laboratory-scale free fall separator. [15] The ore used contained primarily silica and other insoluble with an initial P2O5 concentration of 27.5%. The recovered product had a P2O5 concentration of 33% with a 71.5% recovery.

An additional study of an Egyptian ore with primarily siliceous gangue was conducted by Abouzeid, et al. using a laboratory roller separator. [16] The researchers specifically sought to identify dry techniques to concentrate and/or dedust phosphate ores in districts with water shortages. This study obtained a product with 30% P2O5 from a feed material with 18.2 % P2O5 with a recovery of 76.3 % after careful sizing of material to a narrow range between 0.20 mm and 0.09 mm.

In a subsequent review article covering the full range of beneficiation processes for phosphate recovery, Abouzeid reported that while electrostatic separation techniques were successful in upgrading phosphate ores by removing silica and carbonates, the low capacity of the separators available limited their use for commercial production. [17]

Electrostatic separation of Florida ores was studied recently by Stencel and Jian using a laboratory flow-thru free- fall separator. [18] The objective was to identify an alternative or supplemental processing scheme to the long-used flotation systems since flotation could not be used on the material of less than 105 Μm. This fine material was simply landfilled, resulting in a loss of nearly 30% of the phosphate originally mined. They tested deslimed raw ore, fine flotation feed, rougher flotation concentrate, and final flotation concentrates obtained from two processing plants in Florida at feed rates up to 14 kg/hour in a lab-scale separator. Good separation results were reported with the fine flotation feed (+0.1 mm; ~12% P2O5) from one source which was upgraded to 21-23% P2O5 in two passes with 81- 87% P2O5 recovery by rejecting primarily insoluble silica. Similar results were achieved when tribocharging the feed using either a pneumatic conveying tube or a rotating tribo-charger.

The most recently reported research into the electrostatic separation of phosphate ores involved systems designed to better optimize charging of the materials prior to introduction into a free fall separator, Tao and Al-Hwaiti [19] identified that there was no commercial use of electrostatics for phosphate beneficiation due to the systems low

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throughput, low efficiency and the need to work with narrow particle size distributions. These researchers specifically sought to overcome the low particle charge density associated with systems dependent on the particle to particle contact or impact on a simple charging system. Working with a Jordanian ore with primarily silica gangue, the material was crushed to -1.53 mm and carefully declined to remove material below 0.045 mm. A small laboratory scale free-fall separator was fitted with a newly designed rotating charger designed with a stationary cylinder and a rotating drum, or charger, and an annular space in between. An external power supply was used to apply an electric potential between the fast rotating drum and the stationary cylinder. After charging by contact with the rotating drum, the particles pass into a conventional free-fall separator. Working with 100 gram batch size and starting with a declined feed P2O5 content of 23.8%, after two passes a concentrate with up to 32.11% P2O5 was recovered, though only with an overall recovery of 29%.

In an effort to beneficiate phosphate fines (< 0.1 mm), Bada et al. employed a free fall separator with a rotating charging system very similar to that of Tao’s.[20]. The starting material was from a flotation concentrate containing fines with a P2O5 af 28.5%. A product of 34.2% P2O5 was recovered but again with a low recovery rate of 33.4%.

This “rotary triboelectrostatic free-fall separator” was again applied to the dry beneficiation of phosphates by Sobhy and Tao. [21] Working with a crushed dolomitic phosphate pebble from Florida with a very broad particle size range (1.25 mm – <0.010 mm), a phosphate concentrate with 1.8% MgO and 47% P2O5 recovery was produced from a feed starting with approximately 23% P2O5 og 2.3% MgO. The optimum results on the lab-scale device were achieved when feeding 9 kg/hr and – 3kV applied to the rotary charger. The separation efficiency was reported to be limited by both poor liberation of material in the large particles and interference of different particle sizes in the separation chamber.

Better results were achieved when processing a flotation feed sample with the narrower particle size distribution of 1 að 0.1 mm. With an initial P2O5 content of approximately 10%, product samples were obtained with approximately 25% P2O5 content, P2O5 recovery of 90%, and rejection of 85% of the quartz. This demonstrated efficiency was noted as much better than that obtained with a free-fall separator with a more conventional charging system as used by Stencel [18] demonstrating the advantage of the newly designed rotary charger. Processing a flotation concentrate containing 31.7% P2O5 resulted in a product of greater than 35% P2O5 with a recovery of 82%. This upgrading was noted to be better than possible by flotation.

This laboratory scale separator with a separation system width of 7.5 cm was described as having a capacity of 25 kg/hr, equivalent to 1/3 tonne/hr/meter of width. þó, the reported effects of feed rate on separation efficiency showed that optimal separations were obtained at only 9 kg/hr or slightly over one-third the nominal capacity of the system.

Overall, previous work on electrostatic upgrading of phosphate ores has been limited by the relative charging of complex gangue and the detrimental influence of particle size effects, in particular, the effect of fines. The large majority of work involved only laboratory scale equipment with no validation that commercial scale, continuously operated equipment could be used. Additionally, the low capacities of available electrostatic process equipment have made commercial applications uneconomical.

2. Limitations of conventional electrostatic separation processes

High tension roller electrostatic separation systems as used by Groppo [10] and Kouloheris et al. [11] are commonly used for upgrading a variety of materials when one component is more conductive than others. Í þessum ferlum, efnið verður að komast í snertingu við jarðtengda trommu eða plötu venjulega eftir að efnisagnirnar eru neikvætt hlaðnar með jónandi kórónulosun. Leiðandi efni missa hleðsluna fljótt og verða hent úr trommunni. The non- conductive material continues to be attracted to the drum since the charge will dissipate more slowly and will fall or be brushed from the drum after separation from the conducting material.

Eftirfarandi skýringarmynd (Mynd 2) sýnir grundvallareiginleika þessarar tegundar skilju. These processes are

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limited in capacity due to the required contact of every particle to the drum or plate. The effectiveness of these drum roll separators are also limited to particles of about 0.1mm or greater in size due to both the need to contact the grounded plate and the required particle flow dynamics. Agnir af mismunandi stærðum munu einnig hafa mismunandi flæðisvirkni vegna tregðuáhrifa og munu leiða til niðurbrots aðskilnaðar.

Mynd 2: Drum electrostatic separator (Elder and Yan, 2003 [22]

The limited attempted application to phosphate beneficiation is due to the non-conductive nature of both phosphates and typical gangue material. Kouloheris observed primarily some removal of iron and aluminum containing particles that, due to their conductive nature, are “thrown” from the roller. Presence of this sort of material in phosphate ores is not common. Groppo noted that the only material that was “pinned” to the roller as a “non-conductor” were fines, indicating a separation by particle size rather than material composition. [9] With possible rare exceptions, phosphate ores are not amenable to beneficiation by high tension roller separators.

Drum roller separators have also been utilized in configurations that rely on triboelectric charging of particles rather than charging induced by ionization induced by a high-tension field. One or more electrodes positioned above the drum, such as the “static” electrode illustrated in Figure 2, are utilized to “lift” particles of opposite charge from the drum surface. Such a system was used by Abouzeid, et al. [16] who found that separation efficiency was altered depending on the polarity and applied a voltage of the static electrodes. The Johnson Process [1] used another variation of a drum roller separator. þó, the limited capacity and efficiency of a single roller system leads to the very complex systems such as illustrated in Figure 1. Eins og fram kemur hér að framan, it appears that this complexity and overall inefficiency of the process severely limited its application.

Triboelectrostatic aðskilnaður er ekki takmarkaður við aðskilnað leiðandi / non-conductive materials but depend on the phenomenon of charge transfer by frictional contact of materials with dissimilar surface chemistry. Þetta fyrirbæri hefur verið notað í "frjálsu falli" aðskilnaðarferlum í áratugi. Slíkt ferli er sýnt á mynd 3. Íhlutir blöndu agna þróa fyrst mismunandi hleðslur með snertingu annað hvort við málmyfirborð, as in a tribo-charger, or by particle to particle contact, as in a fluidized bed feeding device. As the particles fall through the

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electric field in the electrode zone, braut hverrar ögnar er sveigð í átt að rafskauti gagnstæðrar hleðslu. Eftir ákveðna fjarlægð, söfnunartunnur eru notaðar til að aðskilja lækina. Dæmigerðar uppsetningar krefjast margra skiltáknstiga með endurvinnslu á miðju broti. Sum tæki nota stöðugan gasstraum til að aðstoða við flutning agnanna í gegnum rafskautasvæðið.

Mynd 5: "Frjálst fall" triboelectrostatic aðskilnaður

Rather than depending solely on particle to particle contact to induce charge transfer, many systems of this type use a “charger” section composed of a selected material with or without applied voltage to enhance particle charging. In the 1950’s, Lawver investigated using various devices including a hammer mill and rod mill to recharge material between separation stages [4] as well as simple plate chargers of various materials. [5] [6] þó, Lawver concluded that material temperature was of overriding importance and particle-particle charge transfer above ambient temperature provided better results than the use of a charger. Ciccu et al. [12] investigated the relative degree of charge transfer and concluded that minor gangue material acquired charge primarily through particle-particle contact due to the low probability of impact frequency with a charger plate. This illustrates a limitation to the use of charger systems: all particles must contact the charger surface so the feed rate must be relatively low. Contact can be improved by using turbulent conditions for conveying the material or by using a large surface area moving charger. The recent work of Tao [19] and Bada [20] and Sobhy [21] use a specially designed rotating charger with applied voltage but only on a very small scale laboratory separator. While this improved charger design has been shown to be superior to older systems, demonstrated processing capacities of these systems are still quite low. [21]

Þessi tegund af frjálsri fallskilju hefur einnig takmarkanir á agnastærð efnisins sem hægt er að vinna úr. Stjórna þarf flæðinu innan rafskautasvæðisins til að lágmarka ókyrrð til að forðast "smyrsl" aðskilnaðarins. Braut fínna agna hefur meiri áhrif á ókyrrð þar sem loftaflfræðilegir dragkraftar á fínum ögnum eru mun stærri en þyngdar- og rafstöðukraftarnir. This problem can be overcome to a degree if material with relatively narrow particle size range is processed. Much of the research discussed above included pre-screening material into different size ranges in order to optimize separation. [5] [6] [7] [9] [12] [14] [16] [19] [20] [21] Á

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difference of 8 að 20 kV. The belti, sem er gerð úr sem leiðir ekki plasti, er stór möskva með um 60% opnu svæði. The particles can easily pass through the holes in the belt. Við inngöngu í bilið milli rafskaut neikvætt hlaðnar agnir eru dregist af rafmagns sveitir sviði til botns jákvæðum rafskautum. Jákvætt hlöðnu agnir eru dregist að neikvætt hlaðnar efstu rafskauti. Hraðinn á samfelldri röð beltið er breytilegt frá: 4 to 20m/s. The geometry of the cross-direction strands serves to sweep the particles off the electrodes moving them towards the proper end of the separator and back into the high shear zone between the oppositely moving sections of the belt. Vegna þess að fjölda agna þéttleiki er svo hátt þátt í bilið á milli rafskautanna (approximately one- third the volume is occupied by particles) og flæði er hrist rækilega, það eru margar árekstrar á milli agna og ákjósanlegur-hleðslu á sér stað stöðugt allt skilur að einstefnuleiðir. The gegn núverandi rennsli sem orsakast af andspænis áhrifamikill belti hluta og þær hinnar stöðugu hleðslna verið mismunandi og með tilvísun til-aðskilnað skapar gegn núverandi multistage aðskilnað á einum stað tækjabúnaði. This continuous charging and recharging of particles within the separator eliminates any required “charger” system prior to introducing material to the separator, thus removing a serious limitation on the capacity of other electrostatic separators. The framleiðsla þessa skiljunni, Báðar línurnar, þykkni og leif, án fóðurmjöl straum. Sýnt hefur verið fram á að vera jafngild um það bil þrem stigum frjálsu falli aðskilnað með fóðurklíð endurvinna Skilvirkni þessa skilju.

Mineral A End

Mynd 7: Fundamentals of STET Belt Separator

The highly efficient separation of particles less than 0.5 mm makes this an ideal and proven option for separation of fines (dust) from a potash dry grinding operation. The STET separator can process a wide range of particle sizes efficiently without the need for classification into narrow size ranges. Because of the vigorous agitation, the high shear rate between the moving belts, and the ability to handle very fine particles (<0.001 mm) the ST separator might be effective in separating phosphate ore slimes where other electrostatic separators have failed.

3.1 Fjármagns- og rekstrarkostnaður

Samanburðarrannsókn á kostnaði var gerð af STET og gerð af Soutex Inc. [25] Soutex er verkfræðifyrirtæki í Quebec Kanada með mikla reynslu af bæði blautu floti og mati á rafstöðu aðskilnaðarferli og hönnun. The study compared the capital and operating costs of triboelectrostatic belt separation process to conventional froth flotation for the beneficiation of a low-grade barite ore. Rekstrarkostnaðurinn var áætlaður með rekstrarvinnuafli, viðhald, orka (rafmagn og eldsneyti), og rekstrarvörur (t.d., kostnaður við efnahvarfefni vegna flots). Inntakskostnaðurinn var byggður á dæmigerðum gildum fyrir tilgátuverksmiðju sem staðsett er nálægt Battle Mountain, Nevada Bandaríkin. Heildarkostnaður eignarhalds á tíu árum var reiknaður út frá fjármagns- og rekstrarkostnaði með því að gera ráð fyrir

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8% afsláttarhlutfall. Niðurstöður kostnaðarsamanburðar eru til staðar sem hlutfallslegar prósentur í töflu 3. Table 3. Kostnaðarsamanburður fyrir Barite vinnslu

Heildarkaupkostnaður fjármagnsbúnaðar fyrir triboelectrostatic beltisaðskilnaðarferlið er aðeins minni en fyrir flot. Hins vegar þegar heildarfjármagnskostnaður er reiknaður þannig að hann feli í sér uppsetningu búnaðar, lagnir og rafmagnskostnaður, og vinna úr byggingarkostnaði, munurinn er mikill. Heildarfjármagnskostnaður vegna aðskilnaðarferlis triboelectrostatic beltis er 63.2% af kostnaði við flotferlið. The significantly lower cost for the dry process results from the simpler flow sheet. Rekstrarkostnaður vegna triboelectrostatic beltis aðskilnaðarferlisins er 75.5% flotferlisins vegna aðallega minni krafna rekstrarfólks og minni orkunotkunar.

Heildarkostnaður við eignarhald á triboelectrostatic beltisaðskilnaðarferlinu er umtalsvert minni en fyrir flot. Höfundur rannsóknarinnar, Soutex hf., komst að þeirri niðurstöðu að triboelectrostatic beltisaðskilnaðarferlið bjóði upp á augljósa kosti í CAPEX, OPEX, og einfaldleiki í rekstri.

4. Summary

While beneficiation of phosphate ores by dry electrostatic processes has been attempted by various researchers since the 1940’s there has been very limit use of such processes on a commercial scale. The limited success has been due to a variety of factors attributable to the separator systems designs and the complexity of the ores.

Feed preparation (Hitastig, stærðarflokkun, ástand umboðsmanna) has a major impact on performance of the separation systems. Opportunities for further work in this area, in particular the exploration of chemical conditioning agents to enhance the differential charging of particles to enable greater efficiency in subsequent separation. The use of such charge-modifying agents may result in processes that can successfully beneficiate ores with complex gangue material, including both silicates and carbonates.

While work continues to further refine these methods, fundamental limitations on the conventional electrostatic systems include capacity, the needed for multiple stages for adequate upgrading of ore, and operational problems caused by fines. In order for viable commercial-scale applications of the demonstrated laboratory techniques, significant improvements must be made to assure reliable, continuous operation without degradation of efficiency.

The STET triboelectric separator provides the mineral processing industry a means to beneficiate fine materials with an entirely dry technology. Umhverfisvæna ferlið getur útrýmt blautvinnslu og nauðsynleg þurrkun á endanlegu efni. The STET process operates at high capacity – up to 40 tonn á klukkustund með þéttri vél. The STET separator can process a wide range of particle sizes efficiently without the need for classification into narrow size ranges. Because of the vigorous agitation, the high shear rate between the moving belts, and the ability to handle very fine particles (<0.001 mm) the STET separator might be effective in separating slimes from phosphate ores where other electrostatic separators have failed. Orkunotkun er lítil, um það bil 1-2 kWh/tonnes of material processed. Þar sem eina mögulega losun ferlisins er ryk, permitting is typically relatively easy.

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Tilvísanir

[1]H. B. Johnson, Processing of concentrating Phosphate Bearing Minerals, Einkaleyfi Bandaríkjanna # 2,135,716, nóvember, 1938

[2]H. B. Johnson, Processing of concentrating Phosphate Bearing Minerals, Einkaleyfi Bandaríkjanna # 2,197,865, apríl, 1940.

[3]O.C. Ralston, Rafstöðuaðskilnaður blandaðra korna solids, Elsevier útgáfufyrirtæki, úr prentun, 1961.

[4]J.E. Lawver, Ore Beneficiation Method Bandarískt einkaleyfi 2723029 nóvember 1955

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