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Publication numberUS2496590 A
Publication typeGrant
Publication dateFeb 7, 1950
Filing dateSep 26, 1945
Priority dateSep 26, 1945
Publication numberUS 2496590 A, US 2496590A, US-A-2496590, US2496590 A, US2496590A
InventorsMarsh Corbin
Original AssigneeAmerican Cyanamid Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Heavy-media separation process for assorting solids
US 2496590 A
Abstract  available in
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Claims  available in
Description  (OCR text may contain errors)

Patented Feb. 7, 1,950

HEAVY-MEDIA SEPARATION PROCESS FOB ASSORTING SOLIDS Corbin Marsh, Old Greenwich, Conn., assignor to American Cyanamid Company, New York, N. Y., a corporation of Maine Application September 26, 1945, Serial No. 618,759

1 Claim.

1 cent years in so-called Heavy-media separation processes. Particularly is this true of the continuously-operating modifications which have been developed. These latter, because of their economy in operation and adaptability to large scale operations, have been found highly advan tageous in the minerals-dressing field.

In such heavy-media processes, various liquids of high specific gravity may be employed as the separatory iiuid. Actually, however, the only practicable uids for use on a large' scale comprise suspensions in water of suitably-sized solids or medium of relatively high specific gravity. A part of this medium is usually colloidal or semi-colloidal in size. Particles in this size range not only remain suspended, but also are capable of maintaining the somewhat larger particles of medium in more or less permanent suspension. By properly selecting the solids, fluids ofsubstantially any desired density can be obtained.

Materials to be separated are immersed therein. Those particles having an apparent density greater than that of the separatory fluid sink therein and the lighter-gravity fraction oats thereon. The light or float and the heavy or sink fractions are then separately, and preferably continuously, collected. Using uids of properly selected density, it is readily feasible to separate solids which differ in specic gravity'by 0.01 to 0.05 of a point.

Because the medium solids have an appreciable real value, they must be separated from the collected fractions and reused if the process is to be economically effective. Again a number of proposed procedures have been developed. It is in this field of recovering and reusing the medium that the process of the present invention has its greatest value.

Despite the obvious advantages of heavy-media separation, it has been considered subject to certain limitations. Most serious of these limitations has been the fact that from a cost standseparation becomes slower and medium losses increase.

Recently, much work also has been done in an effort to extend the size range to include nersize particles without losing the economic advantages of the process. One of the best of the procedures adapted for this purpose is the use of the so-called twin-cleaning circuits set forth in the application for U. S. Letters Patent 2,387,866 to G. B. Walker.y In this process a total ore may be fed, the oatmand sink fractions being separately collected in the usual way; using a magnetizable medium. .The collected fractions are then treated in novel identical circuits whereby a clean, coarser-sized portion is first removed from each fraction and the magnetic medium is then magnetically removed from the small-sized residual particles of each fraction leaving the latter as clean liner-size products.

As noted above, the medium is recoveredv and reused, since without this provision such processes become uneconomical to operate. Walker disclosure and other similar processes, the major portion of the recovered and cleaned medium' is brought to the proper density by the addition of water and recycled to the bottom of the separatory vessel. In practice this presently results in a. gravity differential in the main uid body in separatory vessel between fluid in the 'upper and the lower levels thereof. This differential will increase until a condition is reached at which near-gravity material is too light to be discharged with the sink and too heavy to be discharged with the overflow. Particularly is this nticeable when a wide size-range feed is being treated, including sizes which, because of their relatively large area for their mass, in any case tend to be slow in separating into either the float or sink fractions.

The. process loses much of its 'efliciency and desirability1 under these conditions because of the accumulation of material which cannot be discharged from the separatory vessel. Suiciently powerful agitation to prevent the diierential would interfere with proper separation since a fiow equilibrium is necessary to permit the sink and oat fractions to seek their proper levels. As a result, operation must be stopped until the vessel is cleared of the accumulation. the difierential overcome and equilibrium regained. There remained a demand for some method of preventing the occurrence of this condition.

It is, therefore, the principal object of the present invention to devise a heavy media separation process for asserting solids which is not subject to the objectionable gravity diierential features which characterize the usual practice. Particularly is it an object to devise an overall Ill the operating procedure in which the media solids are recovered, cleaned, and recycled without being subject to this diiilculty' not only when used in' ordinary operations but in connection with Walkers "twin-cleaning process.

Actually and surprisingly, the diillculty encountered with gravity diilerentials in the separatory fluid body may be largely overcome by combining two operating procedures. Both of these procedures involve the use of screen undersize from the drainage screens as medium. These underszes contain medium, water and either ilnesize sink or fine-size iioat particles. In the present discussion these drainage screen under-sizes will be referred .to as sink drainage medium and oat drainage medium respectively.

The first operating procedure consists in recycling the clean recovered medium, which is obtained by any suitable conventional cleaning procedure, together with all or a part of the float drainage medium to the upper levels of the main iluid body, at or near the surface thereof. At the same time suilicient water is added to maintain the desired density value. The second operating procedure consists in recycling all or a part of the sink drainage medium, together with suillcient water to maintain the desired density value, directly to the lower levels in the main duid body. Surprisingly, when it is considered that the primary diiiiculty is due to a gravity diierential and the resulting accumulation of near-gravity and smaller size particles which cannot be discharged, the return of small size particles in the drainage mediums does not aggravate this condition. Actually it has been found that the particles 'quickly removed in normal operation and do not tend to add to the accumulation of solids in the uid.

In thus returning the sink and iloat solids` in the draining screen medium to some level below the surface and a level at or near the top of the vessel respectively, the process differs from the prior art. For example, in the previously identied Walker disclosure, all return is to the bottom of the cone. In other cases, all of the medium may return to the top of the fluid. By the present procedure not only is an additional control of the medium in the vessel eiected but control of the sharpness of separation and the gravity control is simplied.

The invention may be more clearly illustrated in conjunction with the accompanying drawing which diagrammatically illustrates a typical ilow sheet employing the practice of the present invention.

As will be seen from the drawing, the feed to l the separatory vessel comprises a total ore in which the several constituents are present in particle sizes varying over a wide size range. accordance with the usual practice, the heavy fraction settles to the bottom of the separatory vessel and is removed as a sink or underflow fraction and the lighter particles are removed as a float or overow fraction. In the drawing the separatory vessel has been indicated as a conventional cone. However, the process is not limited to this particular type of apparatus and any other suitable separatory vessel may be ach separated solids fraction is then taken to va separate draining screen, the oversize from which comprises particles of the respective "sink and "oat fractions being separated, plus adhering medium. The drainage screen underilows comprise medium, water and ne sink or line tloat." Screen oversizes are taken to washing screens on which the adherent medium and undersize iioat or sink are washed oi, resulting in one case in the production of a coarse, clean sinlt" product, and in the other, a coarse, clean oat product.

It should be noted that, as discussed above, in

:accordance with the present invention the screen undersize from the draining screens is in each .case passed to a ilow divider or splitter from which at least a part is returned to the separatory vessel. That part not recycled directly to the separatory vessel is collected in a sump or the like, along with the screen undersize from the washing screens. The amounts recycled, in the case of the "sink fraction, below the surface of the medium in the vessel and of the iioat fraction at or near the surface, is dependent upon several factors. .These include for example the total amount of Asolid nes other than medium in the iluid; the

amount of fines other than medium which can be tolerated in the cone without slowing the throughput; the viscosity conditions in the cone and the like. In all cases, however, except in starting a new operation, some of the drainings, and preferably for reasons of economy the maximum that can be tolerated, is thus returned.

In an ordinary sink and float" operation, which in the past has been considered to be limited to the treatment of plus l0 mesh particles, there is no problem of the treatment of fines. Consequently the screen underilow from both washing screens would be carried to a common sump and thence through a medium recovery system from which the clean return medium would be returned to the separatory iluid; in accordance with the present invention, being returned to a level at or near the surface of the contained iluid.

. However, the advantages of the present process are even more apparent in treating a full-size range feed using the twin-cleaning circuit of the Walker disclosure as illustrated in the accompanying drawing. Since a total ore is being treated the screen undersze from both washing screens is separately collected. The collected washings are combined with that portion of the respective draining screen undersize which is not returned directly to the separatory vessel.

The sump or collecting tank thus serves the doublepurpose of enabling the collection of the screen underflow fluids and the provision of a steady ilow to the remainder of the .cleaning circuits. Both fluids to be cleaned are first passed through magnetizers which magnetize and coagulate the medium solids'thus facilitating faster settling and removal of water in the thickener to which they then pass. A considerable portion of the water overowing the thickener may be reused for washing, dilution or the like. This magnetic rlocculation and thickening step is preferable, but alternatively, the washing screen underflow may be sent directly to the magnetic separators. In each case the thickened fraction is then subjected to the action of one or more magnetic separators. These may be of any conventional type, as for example the well known Crockett separator which removes magnetically-susceptible -portions constitute medium plus some adherent water. In each case the magnetic separation leaves a concentrate of the fine size particles, in the case of the sink solids, a fine sink product, and in the case of the iioat solids, a fine float product.

Continuing with the medium recovery system, the magnetic concentrates from each set of separators, being substantially free from all solid particles other than medium, are combined and passed through a densier in which the combined material is further dewatered. The normal operation of the thickeners and the densifler results in its being at an appreciably higher density than the separatory fluid in the vessel. Since the medium to be effective must be in a dispersed condition in the separatory vessel, the dewatered medium then passed through a demagnetizing operation. From this point it is normally returned directly to the separatory vessel, as shown in the drawing. It is also possible to send it to a storage chamber, not shown, from which it is drawn as needed. Y Y

As shown in the accompanying drawing, the purpose of the present invention in controlling gravity differentials is obtained by varying several operating conditions. First, the sink solids draining screen medium is returned to the fluid in the separatory vessel below the surface and the float solids draining screen medium is returned at or near to the surface of the contained medium. In each case the amount returned depends upon the setting of the ow divider. The recovered medium from the cleaning circuit is returned at or near to the top of the separatory vessel together with the oat drainage medium, usually being introduced with the fresh feed although for clarity in the drawing it is shown being separately added. In addition, water in controlled amounts, may be added in each case to the drainage medium being returned in order to control the gravity at the desired value. f

In addition to the float solids drainage medium which is returned to the zone of principal separation in the upper levels just below the surface of the separatory fluid in the vessel, there is also returned thereto the cleaned, densied medium from the magnetic cleaning system and if necessary an amount of water. This latter amount of water may be very small or negligible in many cases. By varying the proportional amounts of fluid which is supplied from each of these five sources, it is possible to control the gravity differential without which control the fluid at the bottom of the vessel becomes too heavy and the fluid at the top of the vessel becomes too light. Separation by this procedure may be carried on indefinitely without being troubled by an accumulation in the separatory vessel of excessive amounts of near-gravity particles.

The process of the present invention may be therefore summarized as utilizing:

1. Return of the sink drainage screen medium, which may contain fine sink, below the surface of the separatory fluid;

2. Return of the oat drainage screen medium which may contain ne float, at or near the surface of the separatory fluid; and in addition has as essential distinguishing features;

3. Return of the cleaned, recovered, densied medium at or near the smface of the separatory fluid;

4. Addition of controlled amounts of water to the medium recycled to the lower part of the sep- 5 jaratory uid and, if necessary, to the mediums yadded at or near the surface thereof.

icussed in connection with a particular'adaptain as long as the distinguishing process steps of recycling the medium are present the operation may be varied considerably from that illustrated. For example as noted above, the separatory cone may be substituted by a chamber of any type such as a drag separator or the like. The number and location of the screens, thickeners, magnetic separators etc. may be varied. As noted previously, when the feed contains little or no flnes, only a single medium cleaning circuit is needed. Various arrangements of storage tanks and pumps may be utilized. To escape the necessity of twin-cleaning circuits, the fluids may be passed alternately for fixed periods through the same cleaning circuit for example. 'I'hese variations, however, form no part of the present invention.

I claim:

In a heavy-media separation oi mixed particles of different specic gravities and of a wide size-range by immersing the mixture in a main fluid body, said fluid being a suspension in water of a sufficient amount of finely-divided magnetically-susceptible particles to produce an apparent fluid density lower than that of the highergravity particles and higher than that of the lower-gravity particles; separately collecting the higher-gravity particles which sink and the lower-gravity particles which float and recovering and reusing the magnetizable solids carried therewith from the sink" and oat" fractions: the improved process in which the collected sink" and float fractions are separately drained; a part of the drainings from each said fraction being returned separately and respectively to the lower levels and to the upper levels of the main fluid body; a nte amount of water is added to said lower levels, suicient in amount to maintain the fluid density value in said lower levels thereof; the drained fractions are separately washed, the washings are separately co1- lected; the non-recycled portions of the draindensity of said zone in the upper levels of the Number Name Date 2,176,189 Rakowsky Oct. 17, 1939 2,190,637 Rakowsky Feb. 13, 1940 j 2,206,980 Wade July 9, 1940` 2,379,184 Rakowsky Juno 28, 1945 at the desired value.

fluid of themain fluid body CORBIN MARSH.

REFERENCES CITED The following references are of record in the le of this patent:


Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2176189 *Aug 10, 1936Oct 17, 1939Minerals Beneficiation IncSeparating fragmentary materials
US2190637 *Feb 15, 1938Feb 13, 1940Minerals Beneficiation IncProcess of separating fragmentary materials
US2206980 *Mar 31, 1938Jul 9, 1940Minerals Beneficiation IncGravity sei aration of ores
US2379184 *Oct 26, 1942Jun 26, 1945Reid Janis RProcess for decorticating grain
US2387866 *Sep 22, 1943Oct 30, 1945American Cyanamid CoHeavy media separation process
Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US2623637 *Aug 17, 1949Dec 30, 1952Mij Voor Kolenbewering StamicaSystem of separation
US2692048 *Sep 25, 1950Oct 19, 1954Davis Nelson LMethod for sink and float mineral separation
US2692049 *Nov 14, 1951Oct 19, 1954Davis Nelson LApparatus and method for float and sink material separation
US2726763 *Aug 14, 1951Dec 13, 1955Victor RakowskyMethod of gravity separation
US2821303 *May 6, 1952Jan 28, 1958Davis Nelson LMethod for float and sink mineral separation
US2988212 *Feb 16, 1960Jun 13, 1961American Zinc Lead & SmeltingFull size range centrifugal heavy media separation
US3031074 *Aug 31, 1953Apr 24, 1962Osawa HirosaburoProcess for cleaning coal by dense medium
US7841475Aug 15, 2007Nov 30, 2010Kalustyan CorporationContinuously operating machine having magnets
DE970071C *Aug 13, 1953Aug 21, 1958StamicarbonVerfahren zur Schwerfluessigkeitsaufbereitung fester Stoffe
U.S. Classification209/17, 209/39, 209/38
International ClassificationB03B5/44
Cooperative ClassificationB03B5/44
European ClassificationB03B5/44