Efficiency of the Trent process in cleaning coal

During the war certain suggestions concerning power production were made by Mr. Walter E. Trent to the War Inventions Board, and at the request of the War Department, facilities for experimental work were provided on the grounds of the Bureau of Standards. The Experiments were along the line of controlling the conditions of combustion in a closed space. In order to reduce slag troubles, experiments were carried out for removing ash from powdered coal. After the war, work along this line was continued, resulting in the Trent Process, which agitates or beats together powdered coal, water and oil. A new technology has previously been given to ore preparation by the use of small quantities of oil in water with froth flotation, and although the methods, results and mixtures of the Trent Process were quite different, yet the same physical phenomena of differential wetting was used, and the possibility of there being interesting results in fuel technology was evident. A cooperative agreement was entered into, whereby the Bureau of kines was to investigate the underlying physical and chemical facts and make them public, and the Trent Process Corporation, was to pay the cost of the investigation.

Report No. 261-H-42. Dates August 1,1, 1921. DEPARTMENT OF THE JNTERIOR BUREAU OF MINES H FOSTER "BAIN, DIRECTOR PITTS BURGH EXPERIMENT STATION CHEMICAL DIVISION A C FIELDNER. SUPERVISING cHCMfST EFFICIENCY OF THE TfiEiVI PROCESS Iff CLRAfllflG COAL. fl. St. J.fParrctt and S- P. Eloaay. THE EFFICIENCY OF THE TRENT PROCESS IN CLEANING COAL fey G.St.John.Perrott and S.P.Kinney c < m J by TI S.P.Kinney c > X 55 for the degree of 33 > m 03 CHEMICAL ENGINEER. 1921 EFFlCIENCY by st.John L!:.errott P.Kinney presented S.P.Kinney far CHEMIOAL 1921 Report Ho. 2 61-H-42 Date: August 11, 1?21, DEPARTMENT TEE Secretary, BUREAU MIKES Bain, Director. TEE TEEM IN CLEANING- COAL. lay J. Kinney | Seal $ 1f21, Re~ort No. 26'-H-42 11. 1921~ DEPAR~lEN T OF THE INTERIOR Albert B. Fall, Seoretary, BUR.EA.U OF MINES H. Foster Bain. Direotor. EFFICIENCY OF TI-LE TRENT PROCESS CLEA.NING by G. St. Perrott and S.P.Kinney o Seal' Washington Government Printing Office , 921, description Scope AcJfcnowle&gments Historical Mature mlaeral in apparatus summary Sulphur Amount of oil ueed Oil losses Con Introduction Brief descri~tion of process. Scoj.1e of work AClcrlOw..Lecigments hist.orica.i.. ~&ture of mi~eral matter coal Differences between coal and ore concentration Theoretical Methods and a:p~aratus Calculations of ash reduction and combustible recovery Coals tested Results obtained Brief su.mma.ry Detailed summary Comparison with ordinary washing methods Sul~hur removal General considerations Distribution of forms of sulfur Effect of fineness of grinding Synthetic mixtures of coal and pyrite Synthetic mixtures of coal with shale and gypsum Oils available for the process used in Liethod agitation amalgam grinding statement Methods particles by other workers Microscopic method of classification Calculation elutriation efficiency and grinding reduction Amount of water amalgam l'i~ethod of agi ta.tion Time required for formation of ~ Fineness of gringing General Btat~ent ~ethodB of classifying fine pa.rticles as used ~icroscopic Procedure Ca~culation Comparison with results of e~utriation Relative effioiency of wet a.nd dry grindi-ng Results of measurements Relation between fineness and ash reduotion Fusibility of ash Summary Tables 1• Chemical analysis coals Brief summary results results 4# results Tfloat sink1 jj# forms sulfur grinding sulfur removal coal-pyrite af and gypsum f0 of ¥/ith synthetic 1 Q, Ash removal with diferent oils \\0 \ 2, Details balance 6il loses Importance \5*. Eel&tion 1 6# agitation Effect t£# Time 19# of Ta.b~es 1. Chemioal ana~ysis of ooals tested 2, :Brief s1lllllll8.ry of resu~ts 3. Detailed summary of resu1ts 4, Comparison of res~ts of Trent process and 'float and sink' tests 5, Distribution of fo~s of su~fur 6, Effect of fineness of grindillg on sul.:f'ur remova~ '7, Synthetic mixtures of ooal-and :pyrite 8, Synthetic mixtures caf Pittsburgh coal with shale gy:pS"WD. 9, Analysis of' shale, gypsum, and coal, with synthetio mixtures 10, Ash removal with diferent oils t\, Effect of varying amount of oil 12, Detai~s of oil balanoe sheet 13, Detailed data on cDil~oses 14, Im~ortance of thorough wetting 15,. Reation between size of granules and per cent water in amalgam , 6, Methods of agitation 17, Ef'feot of repeated washing 18, TLme of agitation 19, Sample data sheet showing method o~ estimating average diameter 20, count 2 1 , 22, 23# "by microscopic 2J?, temperature r 20~ Comparison between results of air elutriation and single count-of gross sample 2'~ Comparison of wet and dry grinding 22~ Screen analysis scale. 23. Average size of coal particles as determined by micros,copie estimation 24. Relation between fineness of grinding and ash removal 25, Fusion te~~erature of ash in raw and cleaned coal Elates Plate granules, actual Plates lb, Ic. II» Shaking coal, and oil. III. Churn for $ 0 0 gram samples IV, Churn for $Q gram samples V. Drying still VI. Extraction apparatus VII* Photomicrograph of sedimentation fractions of 200 200 diame* ters. antlrracite magni­fication 200 Photomicrograph and ground Upper magnification 200 r :E~a.tes :P~a.te l. Amalgam gra.n~es, actua~ size. P~ates la, Ib, Ie. II. machine for agitating mixtures of ooa~. water oi~. 500 Brunp~es IV. 50 v. sti~l VII. 2C() mesh anthracite culm, magnification diame: ... terse VIII. Photomicrograph of wet and dry ground anthracite culm at various stages of gringing, magni­fioation diameters. IX. Photomicrogral1h of wet and. dry ground. UPl1er Freeport coal at various stages of grinding, ma.gnification 2JO diameters. Illustrations, % , Relation between size of amalgam and per cent water in 20 Wet dry and coal 3, 4# Water apparatus 3# apparatus 6, screen opening 7# in 34 647 8# in coal, culm No. 7 6?75 f. in coal. % 0, 7 6^74 11 • I~~ustra.tionB. Figure 1# Re~ation between size of amalgam and per cent water retained amalgam 2. wet and ball mill grinding of anthracite culm Upper Freeport bituminous ooal }, Water sedimentation apparatus 4, \i[a.ter elutriation apparatus 3, Air elutriation apparatus 6, Relation between size of soreen o~ening and average diameter of particles 7, Relation between fineness of grinding and per cent ash and sulfur recovered coal, anthracite culm No, 34647 8, Relation between fineness of grinding and per cent ash and sulfur recovered ooal, anthracite cu1m lio. 76975 ~# Relation between fineness of grinding and per cent ash and sulfur recovered coal, Pittsburgh bit­uminous coal, No. 78303 10# Relation between fineness of grinding and per cent ash and sulfur in recovered coal, Upper Freeport bituminous coal, No. 76974 '1. Relation between fineness of grinding and per cent coal, Freeport hone coal Ho. 34645 1 2 , coal, lo. t 3 # fineness in coal, Ho. 75631 1 4 # coal Ho. 7 6027 1 5 # and coal Ho. 7 61 42 ash and sulfur in recovered ooa~, Upper Free~ort bone ooal refuse No. 34645 12. Relation between fineness of grinding and per cent ash and sulfur in recovered coal, Illinois bit­uminous Ho. 75637 13, Relation between finesess of grinding and per cent ash and sulfur recovered coal, Oklahoma bit­uminous No. 7563t 14, Relation between fineness of grinding and per cent ash and sulfur in recovered coal, Indiana bit­uminous coa~ No. 76027 15, Relation between fineness of grinding aild per cent ash and sulfur in recovered coal, Washington bit­uminous ooal No. 76142 Daring certian concerning hy Mr. Trent War Inventions Board, and at the request of the War Dep­artment, facilities for experimental work were provided on the grounds of the Bureau of Standards. conditions in In from in Trent quantities .quite phenomena kines chemici.1 Corporation, was to pay the cost of the investigation. Foreword During the war oertian suggestions ooncerning power production were made by lV'l.r. Walter E. Tre~t to the exper~ental .... ~ .. The Experiments were along the line of cont­rolling the oonditions of combustion a closed space. order to reduce slag troubles, experiments were carri­ed out for removing ash froill powdered coal. After the war, work along this line was continued, resulting the TTent Process, which agitates or beats together powdered coal, water and oil. A new technology has previously been given to ore preparation by the use of small ~~tities of oil in water with froth flotation, and although the methods, results and mixtures of the Trent Process were guite dif­ferent, yet the same · physical phenomona of differential wetting was used, and the possibility of there being interesting results in fuel technology was evident. A cooperative agreement was entered into, whereby the Bureau of ~ines was to investigate the underlying physical and chemical facts and make them public, and the Trent Process -~ several available to any one interested, and are now to be published. While the Bureau of Alines felt justified in investigating the physical phenomena so far as might be done in the labratory, and so far as public interest might reach, no attempt was made to discover the commercial possibilities which development might bring. The question of commercial possibilities must be left for commercial enterprise to answer. consists in water and This partly deashed plastic fuel, called amalgam, the oil selecting the coal particles and largely excluding the water and ash. The water can be freed from the amalgam much the same as butter is worked. The amalgam can be burned in several ways: for example, it may be shovled, or forced thru pipes by pressure; it can be stored also, under water if desir­ed. The labrstory results immeidaily suggest many interesting posssible applications. The severa~ reports as made have been a.ny of. ~,~ines J.abratory, a.nd :public attem~t t~ commercia~ oommeroial comr.aeroial Briefly, the process oonsists agitating together powdered coal, 'water and. oil. ~~1his produces a plastio oalled oan i11. a~so, desi~ ed. labratory ir.umeidally • applucations. wet advantages over dry grinding, provided water can De eliminated afterwards. To able to reduce the ash in coal may make available great quantities of 1m grade coals and material now considered as waste at the mines. If an oil is used which can distilled at a temperature below the coking temperature of the coal, powdered the and the quantity and distilled to dryness, a coke product had no coking quality* If distillation proceeds onl£ to a heavy pitch, a mass suitable for briquett-ing may made. , making, fuel, and gas house tar emulsions can be dehydrated by mixing with powdered coal, the amalgam being retorted for further gas making. Graphite ore can be separated from its gangue, and coke can be separated from flue dust by using the Trent Process. Clean coal in anthracite sludge will make an amalgam if oil is added The brief sketch of possibilities revealed by small scale labratory work shows that the field For pulverizing fuel, v,ret grinding presents many oan b~ be l~w be tile j;)owdered fuel is reclaimed from tb.e amalgam and. the oil may be reused. If a heavy oil is used in suffici­ent may be recovered, although the coal used may have quality. the distilla.tion ;prOlceeds only maSS be made •.. The amalgam can be used for a gas makine fuel t amaleam 1'romflue z will. 0 il development The physically by in particularly and in amalgam, chapters. P.Hood, Chief Mechanical Engineer. for investigation and develo~men.t is large. r:i:he general results show that real benifits are physioally possible treating coal ill this manner. The Bureau has interested itself more partioularly in the ash separation phenomena or the cleaning of coal, L~ the distillation of the ama16am, as outlined in the following chapters • .. O.E.Rood, Chief l!!iechanioal Engineer •. PART I. EFFICIENCY OF THE TRENT PROCESS IN CLEANING COAL by G« Kinney. INTRODUCTION description process.: When of pulverized coal amount 30 cent tne coal* a clean considerable is obtained. The carbonaceous material forms with the oil a pasty agglomerate which is heavier than water, while the mineral matter which was physically separated from the carbonaceous material by the fine pulverizat­ion remains suspended and can be drawn off with the water. This is known as the Trent Process. Scope of Work TREIiT L1 CLEAHllfG G. St. J. Perrott and S. P. Kinney • • Brief desoription of the »rooess, VJhen a mixture of' :pulverized ooal and water is mixed and agitated with oil in an ~~o-QUt equal to }O per oent of the weight of tue ooal._ a. olean sep­aration of a oonsiderable part of the mineral matter oarbonaceous :pbysioally oarbonaceous f~e is ScoRe This study deals with labratory studies Experiments determine oil pulver­ized coal. The experimental procedure followed has sheet of the process. Acknowledgements: Acknowledgement Eieldner Superintendent Pittsburgh Physical samples; W. Petroleum Chemist, for advice during the course of the work and for assistance in testing oil samples; and to W. A. Jacobs, Chemical Engineer, for assistance and advice in constructing apparatus. We acknowledge our indebtedness to E. A. Hartgen, Analytical Chemist, who assisted in the labratory work. r of the efficiency of the Trent Process in separating mineral matter from coal. Ex~eriments have been made to dete~ine for a variety of coals the ash and sulfur removal, combustible recovery, and oi~ recovery ob­tained with different oils, different methods of ag­itation, and various degrees of fineness of pulver­ize~ coa~. ex~erimental aimed to obtain data giving a complete balance shee~ l;lrocess. Aoknowledgement for valuable suggestions and advice to A. C. Fieldner Sugerintendent and Sup­ervising Chemist of the Eittsburgh Station, under whose supervision the investigation was carried out. Our thanks are due to A. R. Powell, £.hysical Or­ganic Chemist , for assistance in determining the forms of sulfur in our coal sam1)les; to E.W'. Dean, J?etroleuI'll. COllrse fo1' assi,stance sBJll:ples; toW. A • assistan.ce ill cDnstructing a];l1?ara tUB. 'IVe F. Valuable preliminary work on the Trent Process was done by H, F. Yancey, Assistant Chemist, and Thomas Frazer, Assistant Mining Engineer, at the Urbana Field Experiment Station, under supervision of E. A. Holbrook, then Superintendant. of the Pitts­burgh Station, HISTORICAL The history of coal washing has been similar to that of ore concentration. Hand picking has been supplanted by jigs, jigs have given way to tables in the treatment of the finer sizes of coal, and of late much attention has been given to the possibilities of froth flotation and other methods making use of the selective action of oils. Bacon and Homor in discussing the problem a. Bacon, Raymond F#, and Homor, William Problems in the utilization of fuels, Jour, Soc. Chem. Ind. , vol June \n9f PP. 161-168T. of the utilization of fuels, describe experiments carried on at the Mellon Institute by Dr. C. B. Carter on the froth flotation of coals. He found that the combustible matter contained in washer wastes of all grades could be almost completely removed by suitable oil flotation, with a recovery of combustible matter preltminary ou Prooess R. Chaaist, Assistam.t Bxperiment su~ervision Station. W8.! ooal, ~ethods seleotive ~, A. Baoon, F., 1JVilliam A., Jour. Soo. Ind., vol. 38, 30, , 919, 1 61 -1 68T. oarried J:,~el.lon B. Carter ~atter oontained ,na tter between and $Q per cent. 3est results were obtained with washer waste crushed to pass a 4b-mesh screen. The floating they were sharp, an&gular and lustrous. Grinding in machines of the disc type to destroy Jhese physical properties and to make the yield of recovered coal from refuse ground in this manner small and its ash content high. Estimates showed that a plant to handle 500 tons daily of ordinary bituminous coal washer waste would cost $ 135.O0& With such and instillation it was estimated that coal could be obtained from refuse containing 7 0 per cent ash to the extent of 73 per cent of the total coal present, in the form of 23 per cent ash concentrate at a cost of $ 1, 84 per ton, Pyrite was found difficult to remove by froth flotation, Ernest Bury^ and co-workers describe an - Ernest: Trans, Inst, Mining Engrs, vol, Q 1?21, 253. carried England, concentrates analyz­ing f-14 40-75 P©r ash. 7 6-8^ betwt:len 70 )0 ,Per Jest crc.shed :;tass 4.6-coal particles showed maximum £~oating properties when antgular lustro'u.s. G~inding machi~es t~e ~hese :properties reoovered oontent Est~ates 5~jC '35,vO~. Vlith instilla.tion wa.s 65-7U 75 I>er present. 25 ~er 04 ton. Pyri te we,s by flotation. Bur~ g Bury, £rnest: Broadbridge, Walter and Hutchinson, Alfred, Froth flotation as applied to washing of indust­rial coal. Trans. illst. TI:.:in:i..ng Bngrs, vol. 60 February 1921. PP. 243-253. investigation of froth flotation of caal ca.rried out at the works of the Skinningrove Iron Company,England. These workers were able to obtain ooncentrates analyz-ing 9-per cent ash from washery wastes containing 41,.1-75 ,Per cent aSh. The tailings contained 76-bY per ash. beleive a considerable of pyrite may be removed by the pfcocess, altho no suirur analysis are given. The washed product, which forms as a thick heavy stable scum on the water surface of the ; froth boxes, contains about j>Q per cent of moisture. This concentrate is discharged into revolving filters of the Oliver type drained under suction, and discharged as a filter cake containing 10 to 1j? per cent of moisture. The cost of cleaning the coal by froth flotation is est­imated at not greater than the cost of jig washing. In regard to the scope of froth flotation in coal cleaning the authors state as follows: " The flotation method does not, of course, compete with washers treating nut coal for sale on the open market for boiler firing, etc. ; it can be employed only where the original coal is fine or where crushing in. part of the normal treatment - that is, for coking, gas-making, briquetting, coal dust firing, colloidal fuel and etc. » v f \-. HATURa OP IvilHEI&L MATTER' U)VCQAL/ , The removable mineral matter in coal consists gypsum, and Calcit and gypsum are usually present in small amounts. Frazer and Yancey ^ discuss the various forms in which ash occurs r cent aSh. The authors belei ve that 8. co.treiderable amount ~yrite ~tocess, sulrur anaJ.ysis ~roduct, scum. VI.'B.ter boxes ,contains .50 15 ~er est-imated v~shin~ sco~e folloVlS: l' co~pete w. ashers maxket etc.; pa,rt trea tillent tha.t gas -meJcing, It ~~ ~ ~ ~ ~ ~~,,;::~~~ .. - 1 - . ~ r_ -' ~ ., .... -;. r : -' __ con~~sts of shale, clay, slate, calcite, gnsum., and. pyrite. Galc~te-­and ill sma~l runounts. ~ coal, removability, «t.. solid pieces ornslate J- inch thick with neutral shale occuring coal mining, a. shale5 1 frozen 1 to the a^acent coal, and thin bands of shale and coal inter-bedded. % friable disintegrate particles occurs in impossible washing , latter Tintrinsic1 words, spearable coal - Thomas, and PI. F., affect coal, Am. l£in. Eng. , bull. 153, p. 1816. in coa~, in order of their removabi~ity, as follows: g Frazer, Thoi.ll.as, Yancey, H. Some factors that affeot the washability of ooal, Inst l'!iin. Eng., 1 5 j , , 81 8. n 1.. Clean so~id pieoes of shale Oi:r-sla,te i- inoh or more thiok Vii th a llB:.utral plane of breakage between shale and coal. This class of impurity includes the definite sl1B.le or slate bonds ocouri~g in the coa~ beds, and extraneous matter from the roof and floor introduced during the mining. 2.. Bands of clean shB.le 1 'frozen • to the ~acent inter­bedded. 3~ Coal, shale, dust and friab~e shales that Aisintegrate in water. 4. Very fine ash ~articles distributed thru the coal, forming carbonaceous shale and bone coal. If ash ocours this form to an excessive degree, it makes ~possible the production of a low ash coal by wa.shing . . . . . . . . . . . . . , These le,tter very finely divided particles of mineral matter are often referred to as 'intrinsio' ash or, in other wordS, ash not speara.ble from the ooal substance by crushing. The intrinsic mineral matter partly of impurities which are intrinsic depends upon the fineness to which the coal is crushed and upon the efficiency of the concentrating method by which sep­aration of the mineral matter from the carbonaceous matter is made. It is difficult to say what is the minimum size of coal that can be improved by ordinary concentrating methods, Frazer and Yancey^ describe experiments in which washery sludge analyzing 12, 8 per cent ash was reduced to B, 1 per cent and the sulfur from 1,7 to 1 , 5 per cent treat-ing on a vmsh-ing table, with a recovery of 5 per cent of the W Yancey, PI, P, loc, cit, clean coal. 48 20- screen per cent 80-screen. Accord­ing Prochaska & in ordinary 10 washing, a Prochaska. Ernest. Goal washing. IvlcGraw 1 s t , 1 ? 2 t f p. r~tter is ~artly derived from the original plant material and partly deposited during the laying down of the coal bed from external sources by sedimentation and precipitation. Obviously the amount im~urities coe.lis cru.shed u,flon mineral; bnproved methods. Yance~~ e. 1 per cent and the 1.7 1,5 treating wash­ing 93.5 ~ Frazer, Thomas and Yanoey, 5. p. loco cit. feed as olean ooal. Screening tests showed that 40 per cent of the material passed a mesh soreen and 35 :per oent passed an SQ-mesh soreen. Accord-ing to Proohaska ~ ordi~ary commercial practice, coal finer than 1 v mesh cannot be improved by washing. L 1?rochasl~, Ernest, Coal wa.shing, IlJl:.cGraw Hill Book Company, 1st. ed. 192\, P. 10, Sulfur Is undesirable impur-ites suitability coke. occurs in and organic In discussing occurence in a says a_ Occurrence fine-ly disseminated Inst, Engre. • 155. 1919. v. 2451. flakes, bo£h in vertical cleavage fissures. But occur microscopic particles, disseminated through the compact coal. This form has little consideration. Finally, coal amiscropic form, microscope coal, coals sulfur pyrite. microns microns, 25 microns; diameter". Su~fur is one of the most undesirab~e impur­ites in coal from a point of view of its suitabi~ity for making of ooke, It ocours the form of pyrite, and. as organio sulfur. disoussing the occursnce of pyrite coal, Thiessen Lsays " It occurs in ~ Thiessen, Reinhardt, Oocurrence and origin of fine­ly diss~inated sulfur compounds in coal, Am. Inst. Mining Engrs,. Bulletin 1 53, '219. :p. 2431. the form of balls, lenses, nodules, continuous layers, thin sheets, or ~akes, boyh horizontal planes and vertica~ o~eavage fissureS,Bu.t pyrites also oocur as very fine mioDosoopic partic~es, or nodules, diss~inated coa~. had very litt~e oonsideration, Final~y, there is sulfur in ooal in amisoropic fo~, ( not visible with an ordinary microsoope ), probably combined with organic matter that exists in the coa~ •••••• All ooals that have been examined by the author contained a varying amount of in very small globules, or particles, of pyrite •••••••••••••••• They vary in diameter from a few miorons to a hundred miorons, the majority measuring from 25 to 40 miorons; relatively few exceed the latter diameter", sulfur the* flakes. Such substance, tendency float coal clean coal concentrate. microscopic particles coal crushing in DIFFERENCES BETWEEN COAL AID ORE COHCEHTRATIOfl certian differences concentrating coal and concentrating ore. In ore concentration gangue and constitutes a small percentage of the total material treated* In coal concentration, the valuable material is lighter than the refuse and constitutes a large percentage of the total material treated. Furthermore, there is a larger difference in specific gravity between values and gangue in ore than in coal, Gangue in ore varies in specific gravity from 2. 5 to 3, 0 and values vary from 4, 0 to 8, 0, while mineral matter in coal ( with the exception of pyrite) varies in specific gravity from 2, 0 to 2, 7 and clean concentrates from 1,2 to 1,7, Again coal contains extraneous mineral matter easily separated by crush- The most troublesome forms of su~fur to remove by present washing methods are the thin sheets and flakes, Suoh plates, even if separated from the coal substanoe, have a tendenoy to f~oat when the ooal is washed and go into the olean ooal oonoentrate, The miorosoopio partioles are not separated from the ooa~ at the finness of orushing employed ordinary washing methods, AND CONCENTRAT ION There are oertian obvious differenoes between oonoentrating ooal oonoentrating oonoentration the valuable material is heavier than the oonstitutes peroentage treate~ ~ ooal oonoentration, oonstitutes peroentage differenoe speoifio ooal, speoifio 2" to 3, 0 and. .v:alues vary from 4. 0 to 8. 0, while exoeption in speoifio 2.0 to 2.7 and olean oonoentrates 1.7. oontains ·orush- intrinsic of pulverization. coal eont-ing varying amounts of inseparable ash, making a clean separation impossible at the degree of fine­ness which is employed with ordinary washing methods. specific man­ifest making processes process, Elmore of oil in a revolving drum. After gentle agitation, the mixture was run into a spitzkasten, where the removed. The ore was separated from the oil by a centrifugal apparatus. Froth flotation, employing an amount of oil equal to about one pound per ton of ore treated or less than the recovery losses in the bulk oil processes, has superseded the Elmore process in the treatment of ore. ing and intrin.ie mineral matter, none of' which can be separtated except by very fine pulverizatio~ The crushed raw coal whivh is to be concentrated may contain particles of ooal of varying gravities cont­ing ~possible em»loyed Any concentrating method which does not depend for separation on spectfic gravity relations of the constituents of the coal, evidently has certian man­iiest advantages. Under this class fall thoes methods use of the selective action of oils. One of the early prooesses of concentrating ores which made use of selective wetting was the Elmore bulk oil process. E~ore mixed the ore with several times its weight of water and an equal weight drwa. ran water and the gangue settled to the bottom and were ]'roth waount 011 of' Process employes considerably less oil 1 bulk 1 oil in commonly accepted bulk oil employed in equal quantity added in an amount equal to 30-40 per cent of the coal. Agitation causes the carbonaceous material form aglomerate heavier while which physically by the fine pulverization remains suspended and can be drawn off with the water. Since is to be different fromthat of the ore con-follow cent rate, it does not necessarily/ that methods using relatively large amounts of oil are impracticable for concentrating coal even though such methods have been practically abandoned in ore concentration practice. The ore concentrate is to be passed thru a metallurgical operation for the recovery of the pure metal; the coal concentrate is to be used ultimately as a fuel and in many cases is to be The Trent PrOcess _p~oyes oonsiderabl.y l.ess oi~ than the Elmore Process and is not a ' bulk I oil. process the commo~y aocepted sense of the term. In the Oi~ process anployed ore con­centration, oil was added in an amount equal. to that of the ore,a sufficient qwantity to cause the whole mass of valuable ore and oil to float on the surface of the water. In the Trent Process, oil is e~l to for.m with the oil a pasty agl.omerate ~eayier than water, whil.e the mineral matter whioh was physicall.y separated from the carbonaceous material tne Sinoe the further history of the coal concen­trate .is to be different fromft.b.a.t of the ore con-o~~ ow centrate, it does not neoessarily/that methods us~g relatively large amounts of oil are ~praotioable for concentrating coal. even though such methods have been practicall.y abandoned in ore concentration practice. The ore concentrate is to be passed thru a metal.~urgical operation for the recovery of the pure metal; the coal. concent~te is to be used ultimately as a fuel and in many cases is to be subjected production coke, pil arid coal. employed considerable percentage pitch, coherent coking ceals, THEORETICAL The Trent Process depends on the same prin­ciples of selective wetting which have made possi­ble froth flotation of ores and have been volumin­ously discussed in the literature of flotation. When oil is stirred into a suspension of coal in water, the first tendency is probanly the formation of an emulsion, with the oil suspended in droplets in the water and the coal suspended in the water and concentrated on the surface of the droplets. The coal particles are, however, so readily wet with oil in preference to water that the globules rapidly become agglomerates of coal and oil. These globules tend to adhere to one another, entrapping water in the spaces between them and forming the pasty mass which preceds the 1 breaking 1 of the mixture. As a result of further agitation, the small agglomerates coalesce into sU'bjeoted to distillation for the produotion of ooke. The mixture of coal and oil may be burned without further treatment or it may be carbon­ized with the formation of coke and the recovery of the p11 and by-products from the coa~ If the oil enployed contains a considera.le peroentage of pitoh, it may serve to make ooherent coke from freely ooking o.als. THEORET leAL prin­aip~ es flotatio~ ooal 14 probably ~ulsion, ·particLes preferenoe thatp. beoome agglomorates anothe~, ru~d Which , , of the mixture. As a result of further ooalesce larger granules finally coalescence point large released "between particles and separate gran­ules visible, agglomerate suffici­ent form mass, Reinders a b have discussed phenomena talcing imiscibie liquids, Depend-a, ReinderB, W, f Die Verteilung Fulvers Oder Kolipid zwisehen I.osungemitteln; Ztschr,, vol, 13, 1^13 PP. 235-41, & Hoffman, F, B, , Yersuche Bentzung uber grenze 2eitschrift fur Chemie vol, 1^13, PP, 385-425. surface solid-solid-oil, oil-t&e (1) *(2) remain ( 3 ) surface solid in ~arger granu~eB and fina~ly coa~eBcenoe reaches a »oint where a ~rge amount of water is re~eased from between the p~rtioles"and the se~arate gran­u~ eB are visibl, with further agitation the gran­ules agglomorate into larger masses and if suffioi­ent oil has been added, finally fo~ a more or less homogeneous mass. Reinders!:. and Hoffman .R h.ave disoussed in some detail the phenomona taking place when finely divided solid is shaken with two imisci"ble liquids. Depend- &. Reinders, W., Die'lerteil.ung eines suspendierten Pulvers oder eines Koll9id gelesten Stoffes zwischen zwei LosUllgemitteln; Kolloid ztschr., vol.13, 1913 23.5-41. ~ Roffman, F. B., Versuohe uber Bent~ung und ubAr das Hoften fester Partiklen and der ·grenze zweier Flussigkeiten: Zeitschrift Physikalische Cheale vol. 83, 19'3, PP. 38.5-42.5. ing on the relative magnitude of the surfa •• ten­sions at the interface SOlid-water, SOlid-oil, and Oil-water, t~. solid will (" remain in the water, i(2) rema.ia in the oil, or 3) remain in the inter­face between the water and oil. According to Reinders, the surfaoe tension relations when a sol.id is shaken with water and oil are as follows: 1. If T~ s. o • .!> T( w. 0'''''' T(e. w), tile solid powder will remain suspended the water. 2. If Tis.w,)^ 3?Cw,©#) ^f(s,o.) the solid will oil, sum solid particles will collect oil These inequalities easily if liquid liquid solid wards solid readily, solid kerosine, oil. substances in coal, calcium sulphate. Calcium while carbon interface. In Process, coal, gypsum, coal comcentrate remain interface. difficulty was later experienced in the removal of pyrite T<s,w, )-t~ T(s,o.) or if none of T( 8. W,) > T{ w.o, ) ..;- T( 8. 0.) the so:lid wi1.l leave the water and go into the o1~ 3. If T(W.O.» T(S.w.,+- T(s.o.) or if none of the three tensions is greater than the awn of the other two, the so:lid partic1es w1ll oollect at the boundry between the 011 and water. ~hese inequa1ities are easi:ly evident 1f we remember that a high tension between a solid and a :liquid means that the l1qaid will tend to assume a spherical shape on the surface of the so1.id or in other wurds will not wet the so:lid readily. Hoffman investigated the distribution of some 25 so1id powders between water and ether, chloro­form, benzol, kerOSine, amyl alcohol, and paraffin 011. Of the substanoes found ineoal, he investi­gated two - carbon and oalcium sulphat~ Caloium sulphate remained in suspension in water, whi1e oarbon concentrated at the interfaoe, our preliminary work on the Trent Prooess, a number of experiments were made in test tubes after the method of Reinders and Hoffman, using finely pulverized ooal, shale, gyp~. and pyrite. These tests showed that ooal tended to caacentrate at the interface or reaain in the oil and that pyrite tended to concentrate at the interfaoe. The experiments foretold the diffiaulty which ooal "by Process, t© specific thru, water globule organic liquid. 'amalgam' a. (I) surface a. In ordinary technical amalgam alley term correctly according 'mixture1, compound, things, ooal oil, (2) coal (3) tension oil in 1 ) (2) is (3) water, 1) (2) coals graphite should readily. (3) form 'amalgam' most surface tension Bet­ween amalgam more difficult. Particles of refuse which from the coal by the Trent Prooess. The pyrite due to greater specifio gravity, tended to break thru. the interface and sink in the .ater surrounded by a g~o~e of the organio li~id. The best conditions for rapid formation of 'ama~gam' ~ of ooal and oil are 1) a low surfaoe .. ordiury technica~ usage, amal.gam refers to an alloy of a metal with mercury, but the te~ is oorreotly- used aooording to Webster's dictionary, to refer to any tmixture', compound. or union of different thingS. tension between coal and oil. a high surface tension between ooal and water, and (3) a high surface tensiOll between oi1. and water. Or ~ other words the reaction will take place most readily ( 1' with a coal which is very readily wet by oil with a coal which 1s not radily wet with water, and with an oil which does not readily form emulsions with water. From(t) and we should expect that the bituminous ooa1.8 and e;raphi 14 shau1.d respond to treatment most readily and the lignites least ireadil.l'. From we should expect gasoline and the higher paraffin oils to fo~ an amal~' ~ost readily than benzol and the higher aromatics and that the presence of substances in water or oil which tend to lower the surfa.ce tenaion .et-ween water and oil would make the formation of the ,\Thioh have physically from, clean ceal preliminary pulverization, if difficulty oil. shale, clay would pyrite in amalgam. Explanation simple attempt should and otner organic t© involved, measurement between organic liquids and water is a simple matter by capillary solid witkdifficulties has been sue ess fully accomplished, a a. Taugl. Jiarl, Experimentaluntersuchungen Oberflaschenspannung flasche fest-flussig; Ann, 1^11, pp. vol. 1^13, PP 1221-A experiments but practical ob-have been physioal~y separated ~rom the olean coal particles by the prel~inary pu~verization, will be easily removed i~ they are readily wet by water in preference to oil and removed with diffic~ty 'if they have any tendency to be wet by oi~. Hence, we should expect that snale, cJ.ay and gypsum woul.d be readily removed suspended in the water but that pyr! te might tend to remain the amal.gam., Expl.anation of the mechanism of the Trent Process is, then, s~ple enough if we do not attaapt to exp­lain why coal shoul.d be wet by oils a.nd otuer organ.io liquids in preference to water or to measure the forces involved. Measure.ent of the surface tension l.iquidsand sUnple the well known capi~lary pipett method, but meas­urement of the surface tensions between sol.id and liquid is fraught witMlifficulties and ha.s not yet sucess~ly accomplishe~ A A Taugl, arl., Exper~entaluntersuoh.ungen uber die Ober~sohenspannUng an der Trennungs flasohe fest­fluss! g.: Ann. Physik, vol. 34, 1911, PP. 311-42; vol.. 42, 1913, pp 1221 -40. number of exper~ents were made with a view to determining the effect of electrolytes in the water, ~t no results of practioal. value were ob- tained, acid amalgam particularly case 0 # \ per cent instead amalgam agglomerating liquid, Harkins has shown that the surface tension of benzeae against water is not changed by the addition of sodium hydroxide to the water. In this case apparently the effect of the alkaline water was to lower the surface tension between the coal and water, METHODS AMD APPARATUS. Goal 65-mesh in the labratory disc crusher. finer meshes the coal in ball and equal weight of water, for periods varying from ex$reemely is desired ( as fine as 800-mesh has been obtained mill into a settling jar. from which after settling has taken place and some of the water has been de­canted, it is transferred to a small electrically stirred glass churn, 300-gram samples of the coal in taine~ It was found that by the addition of acids and aoid salts the formation of the ama~gaa was hastened, ~artloularly in the oase of some of the lignites. If ~ 1 ~er oent solution of sodium hy­droxide was employed 1n~ead of pure water, no amal.gam was formed when benzol was used as the agglomorating liquid. benze.e ohanged ,ll surfaoe water. :All/D AJ?PARA.TUS. Coal is pulverized to pass a 65~esh screen orusher. For ooal is then ground a porcelain bal~ mill with ewwal from" 4 to 60 hours when e:x:jre~ely fine grinding in this manner). The coal is washed from the ball Jar, whioh pla.e eleotrioally sti~red chu~ have been employed most of our work and have U. S. B U R E A U Of- MINES 1455b U. S. BUREAU OF M INES 1455E in churn cc, of sufficient cent coal contain ing cent removable refuse carried small egg-shaped Imown The amalgam and water and suspended refuse are poured onto a 100-mesh screen and washed with water. The amalgam is then placed in the cheurn and washed with fresh water and the process repeated until no further mineral matter is re­moved. products consisting cent water, 2 ) consisting water, (3) consisting process exception retained in the amalgam and filtered refuse, a small amount of disolved mineral matter, and under certian conditions, possibly emulsified oil. can been agitated the ohurn with about 1200 co. of water. A suffioient quantity of oil is added - about 25 per oent of the weight of the ooal oontain­ing 25 per oent removalle refnse - and agitation is oarried on until the agglomorate of smal~ egg­shaped granules known as the amalgam is formed. soreen plaoed oheurn prooess After the amalgam has been separated from the refuse and the refuse filtered on a weighed paper, the produots for analysis are: (1) Amalgam, oonsisting of purified coal, oil, and 10-30 per oent water. ( 2) Refuse, oonsisting of mineral matter, a small amount of combustible matter, oil and water. Refuse water, oonsistiDg of all the water used in the prooess with the exoeption of that ama~ oertian oonditions, Before analysis oan be made, both amalgam oil water. done(in guantative that|oil losses* if separating oil solvent oil, solvent boils than con* and. measured, thus determining the amounts of oil and water in one operation, Dae to the large water in difficulty of accurately sampling the wet amalgam, it has been found more practicable to subject the whole amalgam and refuse to a separate distillation at 110 degrees C. in which the water is cought and measured. The dry material is then extracted with benzol to determine the percentage of oil. When a volatile liquid such as benzene is used in mak­ing the amalgam, distillation determines the am­ounts of both water and benzene and no extraction is necessary. Even when heavy petroleum oils are used in making the amalgam, it is best to dry in a samll still because a small portion of the oil always comes over with the water. Prying in an open dish would thus give rise to an unaccounted loss oil. and refuse must be separated from oi~ and wa~er. This separation must be don~ a ~tative way so that~iL 10sses, any, may be determined. The obvious way of se~arating the oi~ is ex­traction of the amalgam or refuse with a s01vent which disolves the oi~, but does not effect the amalgam or refuse. If the so~vent boi~s at a high­er temperateure tnan water, the water may be con .. · ; densed an~ measured, thus dete~ining the amounts operatio~ Due amount of 'water the amalgams and refuse and the aoouratel.y bas whioh oought ~racted benzol. ~eroentage volatil.e suoh a.ma.lgam,distil.lation andoenzene extraotion neoessary. sti11 beoause a: oomes we. t er. Drying unacoounted for 1.os8 of oi1. In oil 1^-liter Jot ties plate II. Later as/? separation was obtained by agitation in small electrically R. P.M and a capacity of 1500 cct of water, 300- coal I? which ideal for the agitation of 30-gram samples of coal. The volume of the jar is 150-ce. Plate V" shows the still in which the amalgam is dried before being extracted for the determination of oil. The still is kept in an electrically heated oven maintained at a temperature of 110 degrees C, the lead pipe passing out thru an opening in the oven, PlateVI shows a battery of six electrical­ly heated extraction apparatuses used to deter-minthe amount of oil in amalgam refuse. The wiring was so arranged that each pair heaters could be connected in series or multiple, thus giving two degrees of heat. The apparatus may also be used for the simultaneous determination our experiments, agitation of the mixtures of coal, water,and oi~ was carried out in 1~-liter stoppered pott~es mounted on a shaking machine as shown in p~ate I~ ~ater it was found that better ash separation was obtained by agitation in sma~l churns. Plate III shows an e~eotriea~~y stirred glass churn with paddle revolving at about 1000 P.M and a capacity o~ 1500 00. o~ wate~ 300- gram samples of ooal were used in this apparatus. Plate IV shows a mixing apparatus of the type used at soda fountains whioh was found id6al 30-gr~ coa~ To~ume 00. V whioh amalg~ extraoted deteraination eleotrically C. paSSing oven. o~ deter­minthe arrang~d oould oonneoted thuS s~ultaneous deteDnination v SS BBUURREEAAUU OOFf MMIINNEESS 1166660033 J S" RUf: i-Al) Of r."IINI-S 166(l~ uU.. SS.. BBUURREEAAUU OOFF MMIINNEESS 1155228877 and oil. amalgam contained in paper thimble shown in the picture. Benzol is used deter­mine in petroleum cleaners point about 110 degrees C, , is employed. Any modificat­ion E. Vv, Dean a- for the det­ermination petroleum, a. W, , and Stark, D,D,, A convenient method determination petroleum organic emulsions. Jour, Eng. Chem, , vol. 12. 1920. P. 486-498. CALCULATIONS OF ASH REDUCTION AND COMBUSTIBLE RECOVERY In calculating the efficiency of the process, several values are of interest: 1, Per cent ash in the oil^and-water-free clean­ed coal, 2, Per cent ash and sulfur reduction, 3, Per cent combustible recovery* The first two values are qualitative measures of the efficiency of the process. In our work, per cent ash reduction has been defined as follows: of water and, 011. The ama~gam is oontained the pict'ire. Benzol. as a solvent except when it is desired to deter-mine water the amalgam. For this purpose, a grade of petrol.eum naptha known as cl.eaners naptha, boil­ing ',0 C •• empl.oye~ water contained in the material being extracted is distilled over and falls to the bottom of the graduated side tube. The apparatus is a modifioat­ion of that designed by Iv. Dean A,- for the det-e~ ination of water in petrole~ A Dean E,W" D.D" for the deter.mination of water in petro~eum or other organ~o emul.sions. Jour. Ind, Chan" 12~O. p. CALCUlATIONS RECOVERY In oalculating the efficiency of the process, several values are of interest: 1, Fer cent ash in the oil~d-water-free clean-ed ooal.. 2, Per cent ash and sulfur reductio~ 3. Per oent combustible reoover~ The first two values are ~litative measures of the effioiency of the process. In our work, per cent ash reduction has been defined as fo~ows: Ar-Ac coal* per cleaned coal. cent defined am­ount which quality coal than t u e cent elim­ination employed. cal­culated follows: Ac. v clean coal orig­inally by washing percentage considerably higher i f y is amall or, in other considerations cent sulfur reduction, AI:-Ar where Ar is the per cent ash in the raw coal. and Ac the pEr cent ash in the c1eaned ooa1. The per oent ash reduction so de~ined indicates the am-ount by whioh the ~lity of the ooa1 has been improved by the washing process. This seems a figure of more interest and less apt to be mis­leading tL,,-e value for the per cent, el.im­ination often emp1oyed. The latter value is oa1- culated as f0110W8: Ar - 4Q.Y Ar where y is tne per cent weight of c1ean c08.1 in terms of raw coal. This figure is intended to show the percentage of the mineral matter orig­ina11y present in the raw coal which has been removed the waShing process and is evidently always a higher peroentage than the per cent ash reduction as previously defined. It may be very i~ words, if a large amount of refuse has been re­moved. The same consiierations apply to the per salfur reductio~ In calculating coal mind combustion carbon is in determination ash, in determined method, shows £per cent ash remaining after ignition 750 C, contain 15 per cent combustible matter. Several factors contribute to this loss in weight, 1, Combustion of carbonaceous material, 2, 3, Fe^C^ SO2, SO2 formed carbonates, 4, 2 een& shale, in samll in fields, may 50 Parr Inoalculating the amount of combustible matter in coa~ or refuse, it must be born in ~tnd that coabustion of carcon i8 not the sole reason for loss weight when coal is ignited in the analy­tical method for dete~ination of ash. There is always a large amount of mineral matter coal or refuse. This is larger than represented by the percentage ash as detenQined by the ordinary analytical method. For example, a refuse which showsB.5 to constant weight at 7.50 degrees C. does not 1.5 weight. '. material. 2. Decomposition of carbonate, 3. Oxidation of pyrite to Fe203 and S02, and combination of part of the S02 with oxides fo~ed from the decomposition of carbonateij 4. Loss of water of hydration from clay and shale Water of hydration varies from to 12 per cenj; of the Shale, calcium carbonate is present s&m1l amounts the coals of the Appalachian fie1ds , but run as high as .50 per cent of the ash of some of the Illinois coals. Parr: a has proposed the fol- calculating corrected Corrected ash - Asi^ - 3 ^ 3S 0. OB rishw-^4C 8 l~ 1 \ o s jl ~>-irJ Asfe^ per cent at 750 H2SO^ C^ carbon coal. coal. a. Parr, W. , Preliminary analysis. Eng. . vol, 5 1911, P 525 In time in corrected beendetemined 1. 08 ash 2L s Any correction of comp­osition assumptions deriving the the sulfur present organic sulfur formula sulfur correct. COALS TESTED lowing formula for oalou.lating the oorrected ash: Correoted ASilw 3Cl 55 o. 08 tShw-l54Cl 10sj -+-+ L--IT 3 · . . . where ASby, :per oent ash as weighed afetr ignition at.'1.50 degrees C, with addition of H2S04_ c, per cent oarbon occuring as carbonate in the unburned coa.l, S per cent sulfur in the unburned ooal. ~ Farr, S.W •• Freliminary report of committee on coal aulysis. Jour. Ind. and En& Chem •• vol.. 5.'913, ]) 523 our work t~e has not been available for det­ermination of carbonate the refuse and the correoted ash has beendeteI'llined as follows; Ash corrected 1,0,8 ash ~ S 40 Any correotion factor must .of necessity be an approx­imation, the correctness varying according as the o~p­osition of the ash varies from the ass~ptions made in deri yi.ng tne formula. Part of tile sul.tu.r is pres ent as organio sul£ur while the fonau1a assumes the sulfUr is all present as pyrite. Since in general, little or­ganic sulfur is removed with the refuse, the sulfur correction is fairly correot. COALS TESTED Table 1, gives description and proximate analysis of all the samples of coal which have been treated by the Trent Process in the course of the investigation. RESULTS OBTAINED ftrlef Summary: 2 from seem obtained by the treatment of the various coals. In general, best results were obtained by wet grinding of the coal to a siae which would correspond to pas­sing a 600-mesh screen ( estimated microscopically as subsequently described). This gave highest comb-ustable recovery, best ash reduction, and lowest oil losses. The oil used in the experiments in Table 2 was a grade of asphalt base navy fuel oil with the following characteristics,: Specific gravity at 15, 5 degrees C, 0, C# Sayboldt Flash 108 C, Burning point, 128 C, coal ex­periments and agitation carried out in a chum 1. O,BTA.INED Brief Smw'ry: Table 2'gives a summary of those results which fr~ all points of view se~ the best results -by size pas­Sing GoO-microsoopically subse~ently described,. comb­ustable in exper~ents characteristios; 15.5 C. ~ 880 Viscosity at 25 degrees C. 135 seconds Say-boldt ,b'lash point, degrees G. burning pOint, degrees C. 300- gram samples of ooal were employed in all ex­per~ ents churn State County Bed CHMICAL ANALYSIS OF COALS TESTED. a. Source and kind of coal. Locality and etc. Lab Number Penna. Wash, Pierce Penna. Beaver Fgh, Allegh- Upper eny Free-port, wn it 111. Ind. Willi­amson Macou­pin Sulli­van, No. Culm- sample from Trent Process Corporation, Washington C# 34647 Culm- feed to concentrating tables Coal Co,, Scranton Pa. 76^75 Sample from Trent Process Corp­oration, Washington, D.C. 7 8127 SEMI-ANTHRACITK Run-of-Mine coal from cars in mine at working face, Carbon Hill Coal Co, , Carbonado, 7 6t 41 BITUMINOUS Fee* to washery, Jones and Laughlin Co., Woodlawn Pa. 75835 Pulverized coal from Oliver Iron anc Co. Pa. Feed to washery, Inland Collieries Indianola. 34 643 Washed coal from aoove, 34 644 Run of mine coal, Avenue mine Co., 7 6^74 Run of mine. No,7 mine, Muddy Co, , Hevrin, 7 Run of mine No, t. Mine Superior Coal Co., Gellespie, Run of mine,No, 12 mine, Vandalia Sulivan. 7 6027 Bid J?enila, " R. I. Wash. Fierce ~ '~ Psh- It" n 111.. Ind. ; / " " ..H'ree­port, " It " " Wil.li- 6 ameon Maoou- " pin Sulli- n van.. WLE 1. CHmICAL A lj/iLys I§ COAlS mTED. ooal.. Lo0ali tz ANTHRACITE Prooess Wash~ton D,C, . Hudson Oou <Co,,,. Soranton Pa, Sam»le Prooess D,C, SmI-ANTHRA.C IfE, coal. 'Working Hil.l Co., Carbonado. BIQDiOUS Fee6 Pap Pu1verized anc Steel Co, Pittsburgh, Ea. Company, Indi&nGl.a. coa~ ~rOlli aDove. ooal, Allegheny Steel Co" Breokenridge, No.nine, Big ~uddy Coal and Iron Co., Hevr~ No.1. IlJJ.ine }4647 76975 78127 76141 34867 34643 34644 76974 75887 Co,. Gellespie. 75637 NO. Coal Co., Suli van. 7 6027 . Lak lfon Tenn, Hamilton Ala, Okla. Uew Mex, Wash, Pierce Tenn, Ala, lew Eex Wash, Beaver Hamilton Walker . Colfax Black Lehigh morris BlOSS-burgh. Free-port Fgh, Soddy Black Bloss-burg Lewis sleek. Mine Durham Coal and Iron Co, , Soddy 73823 Washed, from above, 77MO Run of mine, itto. 2 mine, Black Creek Coal Co,, iiauvoo, 736BI Run of mine coal, Ho, 2 mine Folsom Coal Mining Co,, Lehigh, 73631 Washed Co, f Dawson, 77338 coal, Wilkenson Coal and Coke Co,, Wilkenson, 7 6142 Uon coking coal, Co. , Carbonado, 7 61 83 Washington, D#C, 6023 Co, , Harmarville, 34643 Washer refuse, Jones Laughlin , Woodlawn. 78386 Washer Co, , Soddy, 77341 Greek Co, , lauvoo, washer Co., Dawson 77339 BITUMINOUS Mendota Co,, 7 6184 State Tenn. n Al.a. Okl.a. New .lVlex. Wash. County Bed Locality and etc. Hamil~on Soddy Unwashed nut and slack, Soddy mine Durham Coal and Iron 0-0., Soddy Walker Coal Colfax Pieroe n Washed, from a Dove. Blaok Run of mine, 11l0. 2 mine, Jjlack Creek Creek Coal Co., :liauvoo • .Lehigh Ru.n 0 f mine coal, .No. 2 mine Fo 180m Morris Coal l~Lini.ng Co. J Lehigh. Bloss- WaShed coal, Pheleps Dodge Co. , burgh. Dawson. Coking 00&1., run of mine, Wil.kenson Coal and Coke Co., Wilkenson. Non ooking ooal, run of mine, Carbon Lab. No. 7,5825 77540 756131 7,5 631 77538 76142 Hill Coal Co., Ca.rbonado. 761.85 Brazil Alleg­heny Sample from Trent Process Corporation, Wa.shington, D. C. 7 602.5 Penna " Tenn. . Ala. New Mex Wash. " Heaver Upper .lfree­port Pgh. Bone coal refuse, Inland Collieries Co., Harmarville • washer re:t'use, J' ones and laughlin Co. , i~ood1.awn. Hami1.ton Soddy 'washer refuse, Durham Coal and Iron Co., Soddy. Black. Washer refuse, Black Oreek Coal Co., Creek Uauvoo. Bl.oss- Washer refuse, Phelps Dodge Co •• burg Dawson .Lewis SUB-BlTU.lildNOUS Run of mine from bins at head of washery, ~endota Coal and Coke Co., Mendota. 34645 '7754\ 77846 77539 76184 State , Xflfr. IP.- Wash. King - Run froil plus hone picking . Pacifio Coast Coal Co. Issaquah, 73897 LIGIITE Texas - Run Ho, 1 Bertetti Coal Co. Lytle, w Milain - Run Lignite Co, , Cal. - Co. , lone H, D, - - Run of mine coal, mine unknown. PROXIMATE ANALYSIS Lab, no. Condi­tion. Mois­ture. Sulfur. 3 2,13 7. 27 7. 43 10, 28 64, 83 #9.72 27.14 27,74 1, 1.39 6975 3 1 . 15 7/98 8, 07 11. 78 39.72 60, 42 $8. 22 31. 15 31. 51 1. 72 2. 54 78127 3. ^ \\9yQ 12-33 14 03 62, 50 63.72 83.97 60 21,73 . 81 • 85 1. 09 7 6141 1 2 3 8,77 ,8,92 10. 20 77.17 78, Ay 89. 80 12,53 12, 59 . 52 . 53 . 61 78383 1 2 3 1. 33 33. 34. 14 39. 03 32. 37 33. 29 60. 93 12, 13 12, 1.73 75 2, 02 75823 75824 76026 75472 StAte County Bed Locality and etc. .. lAb. lio.- of mine fr~ bins at head of washery plous bone from pioking table, Pacifio Coast Coal Co. Issaquah.. 73897 LIGNITE Medina of mine coal, l~o. , mine, .tiertetti Coal Co. Lytle, 1t Mila in of mine, Rockdale mine Rockdale :Lignite Co., Rockdale. 15824 Amador Run of mine, McKissick Cattle Co., lone .N. D. Run of mine ooalo, mine unkno~ 73472 PROXThI1A.TE ANALYS IS Lab. Condi- Mois;..; Volatile Fixed No. tion. ture. Matter Carbon Ash Sulofur. 34647 1 2, 1.5 2'1 63.44 27. 14 0,98 2 64. 27.74 1. 00 3 , 0, 2B 89.72 1, 39 7 697.5 1 " 1 .5 7.98 .59. 72 3t. '.5 '.72 2 8. 01 60,42 31, 51 1.74 3 ".7 ~B. 22 2, .54 1 .5 • .r!U 1 ,. ~tJ 62.30 20. , 81 2 '~55 65.72 21.73 • 85 3 , 05 83. '7 1.09 76141 , 1, 3'l. 68 1:088...729720 178S79... 8147~0 ,, 2~ •. .5593 ••• .565132 7838.5 , '. 3.5 3). 68 .52. 12.13 1. 73 ~ 34,14 .53. 2'7 , 2. 30 1. 7.5 39. 0.5 60.95 2. 02 Lab Condi­Mois­Volatile Fixed ture Sulfur 1.53 33. 52. 72 12,33 1.25 2 33.94 55. 54 12. 52 3 38. 80 61. 20 - 1. 45 1. 30 34. 05 55. 50 9.35 • § 4 2 34. 50 54 47 . 85 38.11 61. 89 - . 94 1. 40 5 4 9 6 4 1 2 . 72 36. 02 57.77 4 . 75 3 38. 40 61. 06 - ••• • 78 7 6974 , 55.40 7 . 95 2 . 19 3 4 1 4 55. £5 £.21 39.29 - ' 2. 40 75887 52.42 9. 93 1, 28 5.7-8 55. 10, 45 1. 36 37. a? 62, 1 8 - 1.52 7 5 637 1 4.95 5 7 . 40,77 1 4 55 5. 33 2 39. 60 42.90 5. 61 4b. 06 4 79 7 6027 2.45 42, 45. 37 9. 4.27 2 43. 87 4, 3-8 52.1 6 4. 86 75825 82 58. 40 14, 30 1, 02 29. 24 59. 25 14, 51 33. 04 64 96 - 1.1 77540 . 7 3 27. 13 5 9 . 12,98 . 71 2 27.34 59. 58 13. 08 . 72 45 68,55 - .83 75681 44, 20 4 65 1. 52 • 2,9B 47. 59 45. 56 4 85 3 51.09 48,91 1. 69 Condi- M.o1s- Vo1atile :i'ixed No tion ture Matter Carbon Ash SulfUr 34.861 1 1. 53 33, 42 7,2 12. 33 1. 2.5 53. 1. 27 :; 38.80 ~O 1 .45 34643 1 1.30 0.5 30 9. 35 84 .5 6. 03 9. • 8.5 3 38. 11 .94 34644 1 35. 52 56. 96 6.12 .72 2 57. 77 6. 21 .73 :; 38.40 61.06 .78 76974 1 • 80 35.85 7.95 2.19 2 3£.14 .75. B5 8.01 ~. 21 3 .39. ~9 60.71 2.40 15881 1 5. 7 B 31. 87 .52. 42 9.93 1. 2 33. 83 .55. 63 10. 4.5 3 37.8Z 62,18 1. 52 75637 4,"} 5 37. 75 40,'.17 , 6. .55 4a.~o 17. 41 3 4b• 0 6 .5h 94, 6. 76027 1 2. 45 42., 07 ~,. 87 9. 63 4. '2.7 43, 12 47. 01 9. 4.38 3 47. 84 52.16 7.5825 1 1.43 28. B2 .58. 1. 2 .5~ 25 1 4 • .51 1. 03 3 33.04 6 96 1, 1 6 77.540 1 .73 .59. 14 12.98 • 71 '27. 34 5~. 58 13.0B .72 3 31. 4.5 6 • .55 1 2,)18 46,17 44. 6. 1 • .52 2 47.59 4.5. 56 6. 8.5 1. 57 :; .51,09 48.91 1, ff) on&i-tion Mois­ture Volatile j&atter Ash sulfur 1 2 3 ' 3. 78 35. 33 3 4 7,4 45. 62 42. 14 43.79 54. 38 1 8 . 73 47 4. 56 4.74 89 2 3 37.27 66 41. 58 52. 37 52.91 58.42 9. 33 43 .66 . 67 . 7 4 1 2 3 1.53 30.07 30. 54 41. 78 41.90 58.22 24 50 2 4 9 1 .85 1 2 3 7. 37 25. m 43. 39 34 46 5 4 61 32.98 55. 60 2,29 2. 47 2.84 1 3 1. 29. 30,12 38. 49 47. 48. 14 61. 51 21, 42 21. 74 , 9 2 . . 93 1. 19 1 2 3 1. 05 33.58 01 42,70 43. 15 3.28 5. 82 3 . 80 6, 48 45. 10 1 9 . 90 34,90 62. 95 63. 46 1. 63 1, 4.49 1 3 30. 31.38 41. 44, 42 4 5 . 16 59. 00 23, 08 23.4 6 1.57 1. 2, 09 1 2 1.03 37. 41. 58 52. 37 52.91 58.42 33 43 . 66 . W . 7 4 1 3 14. 03 34 52 48 50. 05 34 45 42. 40 49.95 13. 00 1 5 . 1 2 1, 04 1. 21 1.43 Lab. Condi- Moi.- Volatile Fixed !ic .. tiOll ty,re Mtter Carbon Ash SUl.f'ur 75631 , 3.1-8 35.33 14 18 .. 73 4 .. 36.14 43,79 19. 47 4.14 3 45. 62 5. 8, 71.538 1 1.03 37. 27 52, 37 9.33 • 66 2 37. 66 32. " 9. • 67 3 41.58 58. 42 .74 76142 , 1 • .53 30,07 41,90 26. .60 2 30, .54 42,55 26.91 • 61 3 41.7 B .58. 22 ,8, 7 602.5 , 7.37 23, 86 33.77 2. 29 2 27.94 36.46 35. 2. 3 43.39 56. 61 2,84 3464.5 1 1• 48 2~. 67 41. 43 • ';12 2 30.12 48, '4 21.74 .93 '\ 3 38,49 61 .. .51 1, 78386 , " 0.5 23. 03 33. 22 42.70 3. 28 2 23.27 33. 58 1.5 3. 31 3 40.93 59. 07 77.541 1 • DO 16.35 19.90 62., 93 2 1 6. 48 20. 06 63,46 64 3 45.10 5<\,90 77864 , 1. 63 3D, 87 44,42 23. 1. 57 2 31. 38 45. 1 6 23. 46 1, 60 3 41, 00 39.00 2.0? 77539 , " 03 ~7, 27 9. , ~6 37. 66 52. 91 9. • 67 3 41 • .58 58,42 .74 761 84 1 14,03 36. ,52 36.4.5 13. 1, 2 42. 48 42,. 40 1 .5. 2 '. 21 3 30. 0.5 49. ').5 1. 43 Lab, No. Condi­tion Mois­ture Volatile Matter Fixed Carbon , Asia Sulfur 1 10,63 34. 97 37.12 17. 28 . 43 2 39.13 41. 53 19. 34 .48 3 48, 51. 49 - , 60 7>823 1 2 4 31.97 2 4 80 1. 3 4 21 20. 19 1.92 3 45. - 75824 32. 1£ 07 7. 28 . 88 48,7 6 40. 10,73 1.30 54. 62 54.38 1. 46 'I 6024 15. 20 48. 31 21, 29 15. 1, 60 5 4 ^5. 11 17. 92 1. o> 6?. 30, 59 - 2, 3S 7 5472 1 18, 37. 40 34 82 .87 2 4>. yo 25 1 .07 50, 59r - 17 condition, coal received, indicates moisture-free calculated Lab. Condi- lVlois- Yo1atile No. tj.on tYrre 1\jJ.a.ttgr Ash 75897 12 10. 63 33~4., 9173 3471.. 1532 117?. 3248 •, 4438 3 48. 51 51.49 ,60 '15823 , 26. 68 31,97 26. 65 14. 41 2 43. 60 36.21 1" 1. 92 3 54. 63 4.5. 37 2. 41 7.5B24 1 32.1B 33. 07 27. 47 28 • 88 2 48.76 40, 51 10. 73 1,30 3 .54. >4.38 '1602.4 1 1.5, 20 4B.31 21. 2.9 1.5. 20 1. bO 75472 2 56. 97 iC5. 11 1. 07 3 (fj. 41 30. 5~ 2.36 , 1.8. 63 37.40 36. 7. 1 5 • 87 ~ 4). lO 45. £.5 8.79 .01 3 50. 3'- 49. 61 1. Note:Under oondition, 1 indicates the analysis of ooal as reoeived, 2 indioates the analysis calculated to moistUre­free basis, and 3 indicates the analysis caloulated to moisture ans ash-free basis. Efficiency (Dime of Ash Redue-Combustible Sulfur Oil Rec- Agitation f Recovery » Reduction * every <fe TTgmi>w_ 73. 0 69.1 53.9 49. 6 21. 0 11. 1 6. 2 5 1 .7 62. 8 3 4 50. 4 22. 9 52, 2 54. 8 49. 0 39. 8 5 3 .5 72. 2 43.7 67.7 72. 0 58.1 45. 0 48. 2 44 o 26. 8 98, 8 25 98.5 43 98. 0 99.1 2 99. 0 99.\ -13 100. 0 99. 8 100. 0 8 - 99, 4 99--. 9 206 111000000* 94. 9 85. 99. 8 100 98. 100 99.1 - 1 100 99. 6 - 1 100 99.9 88. 1 12 100 -1 88, 9 98. 9 - 2 98, 97. 9 4 9 100 26 9 7 .7 99. 5 77. 2 10 100 100. 0 82, - 10 100 -56 9 5 .5 99. 99. 2 0 - 4 100 100. 0 1 •98,9 12 99. 0 1. 0 . 7 2, 0 . 3 1. 0 1.0 f.o 3.0 0, 0 1.0 : .7 2,0 1, 5 5.0 2.5 .3 . 5 1.0 . 5 2, 0 1.0 2, 0 3.0 .8 1. 0 1.0 . Ash Reduc-Combustible Sul.fu.r Oil Rec- ATigmiet aotifo n tion l' Recoyery 1? ReduQt~on ~ overx ~ HQurs. 67. 8 98.8 25 99. 6 1, () 7639.. ,0 '998.• '.15 432 '>9'89.. 00 2•. '(1} 53. ? 9?, , -13 , 00. 4'9. g 3 1•. 3(}- 53. 8 99. 8 - 6 99. 4 1. 0 "1'7. Ij " 100 1. 0 3 6 100 1. 0 1 6. 2 2 100 j.O .51. 7 ,4,9 8 3.5. 5 , 0.0 62 8 '/- '''j B - 3 1. 0 . 36•. 4 9B,3 3 .7 50. 4 99. 1 - , 4.0 2.2. '1 -, 2.0 52. 2 1. , 54, 8 19 88,9 5. (} 49.0 99. 6 6 98. 5 2, .5 39. B 98.9 98. 5 • 3 .5 3. 5 97, 5 -46 • .5 7~ 2 96.9 97.7 1,0 43. '1 9;;, .5 19 99. • .5 67. '1 71. 8 '00 2, (} 72.0 1, 0 58. , 82• 8 -.5 6 9.5 • .5 2.0 4.5. (} 99 •. 8 - 3 951. 2 3.0 4[3. 2. 99. (} , 00 • B 46. 0 , 98.9 1. 0 26• 8 94,9 ~7. 0 1. 0 Kind of Coal TABLE II BRIEF SUMMARY OF RESULTS. Raw Coal Cleaned Coal Lab, Sulfur Weight Ash Sulfur Weight Ash $2. % Anthracite Culm « Tf R, I; Anthracite Wash, Semi- » Pgh, Bituminous Upper Freeport It I! 111^ Bituminous Ind, Twe nn, Ala. Oxla. K, Hex, Wash, n Pgh, washer Ref, Upper Freeport bone, Tenn, bit, washer ref, Ala bit. " « if, Hex," « « Wash, Sub-bit, Texas Lignite Cal. » 34 647 27, 7 1, 00 7 6 9 7 5 3 1 . 5 1,74 78127 2 1 * 7 0, 85 7 6141 12. 6 53 J * 1. 75 34867 13. 0 3 4 643 9.5 ,85 34644 4 2 # 72 8,0 2.34 75637*^61 75887 10. 5 1. 36 7 6027 9. 0 4. 3 b 7 5835 14. 5 1,03 ,72 75681 4 9 1. 38 75 631 19. 5 4, 74 77538 9. 4 , 67 7 6142 22, 6 49 7 61 83 24 9 .61 78386 3 4 64 5 21. 7 .93 77341 63. 5 1. 64 77 864 23.5 1, 77539 54.7 .33 7 6V84 15.1 1.21 75 897 19. 3 . 48 7 5 8 2 3 3 3 , 5 1,44 7 602 6 3 5. 1 1.77 7 4 5 71. 0 82. 0 91. 0 92. 9 1 . 97. 5 98, 4 98.5 84,0 95. 2 90, 5 94 0 7 4 0 6 88.7 80. 0 59. 0 88. 4 31. 80. 5 45. 90, 0 88.0 79.7 81.5 8.9 8.5 4 7 5.8 4 2 4 0 7. 5 5. 5 £ 7 8.4 3.9 4 3 7. 2 10. 1 3.3 8. 8 4. 13. 6 12. 5 12. 2 6 4 6 22.9 8.3 10, O 18. 25.7 1. 00 . 83 . 60 1. .85 . 68 2. 30 5. 15 27 1. 04 . 7 3 1. 39 3. 85 .80 .50 * • 2.45' 1. 1 . 76 . 83 1.23 - . 50 1, 1. 56 23.5 29,0 18. 0 9. 0 8# 0 8.5 2 .5 1. 1 4 0 8, O 4 ,8 9.2 4.0 4, 0 24, 0 5. 11. 3 20, 0 41, 0 11, 6 69. 55. 0 10. 0 12, 0 20. 3 18,5 84 88. 90.7 84,5 90. 0 88, 87. i 65. 90.5 84 2 85.1 89. 6 53.7 84 85.2 84. 2 87. 2 88.0 82,7 80. 6 80. 84 94. 2 7 5 .9 • • T!bLE II BRIEF SUlltJ.J.Iil.ARY OF RESULTS. Coal. C'l.eaned Coal. Refuse ~. ..... ...-..~+ . Lab, Ash Sul.: lifo, .'fo: 20 % % % ~ % ~ ,. 34647 27.7 00 76..5. 8" ~ .75 23 • .5 8.8. 6 1.", tt It 6975 31. 1.74 0 8 • .5 00 29.0 88, 0 }" WR. aIS;h . ASnetmhri-acn ite '7186114217 1212 ... 76 O•. .8553 9812.. 00 56. .7E •• .6803 198.. 00 9840• . 7.5 •" Pgh. Bituminous 78385 , 2 .. 3 1. ·1j2. 0 ~2 1, 69 8.0 89. 5 1. tI It 34867 13. " 1. 1 6 91. 5 6.0 1. 23 8 • .5 90.0 • 346431 • .5. " 85 97 • .5 7 • .5 • 8.5 2.5 8a 0 .. " n 6. .72 98.4 5 • .5 " 68 1" 6 -- - 11 It 76974 B. 0 98" 5 6.7 2.30 '. 5 87. 6 - 11.l. .8i tuminous i, 5 637 t 7. 4 .5. 61 84.0 8. 4 6. 0 f>5. 5 B • 11 n 1 G. 36 92. 0 1. 40 8,0 '~O" 5 Ind. II 76027 9, ts '95, 2 6.3 4. 4.8 8-6. ~ Tenn, II 758?5 14. 1, 03 90.5 '. 04 9, 2 84, 6 • 1t " 77540 13. 1 .72 96.0 , 0" t .73 4. 0 85. , • Ala" n 6. 1" .58 ;16. 4.0 89.6 3. Okla, It '1 5 1 9, .5 4.74 76.0 8, 8 24" .53. 7 1" .l.II, M.ex. lJ 9.4 • 67 94. 6 4 .. 8 " 80 4 86,. 6 ~Vash. n 76142 22. • 49 88. 7 13. 6 1 t, 85.2. u 85 2. 6. • 61 80. 0 12, 5 .. R(}l 20. 84 " Pgh. Ref. 7B386 43. 2 3, 31 59. 0 12. 0 2 • .45' 41.0 87•. 2. 3". bone. 34.645 21.7 • 'if 3 88. 4 1'"-.1 t:':. ,75 116 2. Tenn. ref. 77541 31. 0 20. 6 1• 48 tIJ•. 0 82, 7 1" n n 77864 23. 5 1. 60 80 • .5 6. 6 '.76 19. 5 92. 8 life Mex" n n 1I 54. 7 • ).5 4.5. 0 22. )l • 8.5 5.5. 80, 6 " v~ash. tit. 761 84 1.5. 1 1. 21 ;)0.0 8. 3 1. 25 80, 0 '. n II t1 T5&J7 19.3 • 48 88. 0 10, 0 • ,SO 12. 86. 3 ., 75823 33. 5 1. 44 79. 7 18. 1 1. 42 20,3 94.2 1., Cal. n 7602635. '. 77 81. 5 2.5. 7 1 • .5 6 , B. 5 75. 9 2" I~ in £late I I I . All results moisture-free basis. in Table 2. and gives a detailed summary of all the experiments carried out in the course of the investigation with the exception of certian experiments dealing with particular phases of the Process and discussed subsequently. The amount of oil used has been figured in gallons per ton of dry raw coal. Under type of agitation, 'shaker' indicates that the experiment was carried out with 300-gram samples of coal in 1^-liter stoppered bottles agitated on a shak­ing machine as shown in Plate II; 1 small churn1 indicat­es that 30-gram samples of coal were used and agitation was carried out in the mixing apparatus shown in Plate IV;, 1 large churn1 indicates that 300-gram samples of coal were used and agitation was carried out in glass churn shown in PlateV, A figure in brackets ( ) for per cent sulfur in the refuse indicates that no analysis was made, but that the calculated figure indicated was used in the combustible recovery calculation. Under 'sulfur reduction1 a minus figure indicates that the sulfur content of the clean coal is higher than that of the raw coal. The remainder of the table is self-explan atory. shown flate IIi. A~l reau~ts are expressed on the moistuxe-£ree Detailed Summary . Table · 3 includes the results Tab~e 2, B.nd o£ eXlleriments exper~ents partic~ar disaussed subse~ently. coa1. shaker' indioates exper~ent s~ples 1i-Shak­ing 'churn' indicat­es 8.11paratus I large churn' indicates that }OO-gram samples of PlateV. gulfur cal.c~ation.. sulfur reduction' the. t expL&n .. ~ .:. :J.~P'...~. ,:.: ". ~. Kind of Coal 2. Lab, Thru lumber Particles o n m. Gal. Type of Per Agi- Exp- Ton tat- eri- £ind ion, ments 9 10 'I Cor1ed f> 1° Anthracite Culm, Bit, 18385 34643 34647 65 133 it H.n F. 56 11 S sc 2 1 3<V4 1. | 1 .» n C. T, n 11 1 n IT 200 I.F. s 10 w 11 ; 1 1111 1i1t Ew IITI LscC 12 «w 1111 F 11 n H B 11 1 11 ir T if n n If 1 ii 11 1 ft n C. T, 11 2 w w 1 w w I . P. s 1 tl f! * 0 11 s 2 tl if 1 10 H.F. s If if 1 nn 99 wB 1if1 SLCC 23 11.11 ttl t IT 900 ii 11 1 u it 1 76975 65 130 11 11 1 3 1 .5 31W 200 35 w 11 11 1 600 H.F, 70 1 f If 1 n 9 g . o . 70 n 2 v.S If T 7 8127 550 11 11 2 1 .7 8 0 * 7 6141 200 35 11 1 12, 13.9 • t 550 it 11 n 11 1 it if 1 11 11 11 1 11 fi t 7 83^5 B 1! SC 1 12, 3 T4, 2 1 . ' it H, F, 11 11 1 w . ii 1. 200 35 11 11 1 ri 11 f if 35 If. F, 11 SC 1 11 Tl Tl 7 00 200 6 11 109 LC 4 11 IT f 35 B 79 s 1 2 ,5 tl nii inf TF,. T1l1 1111 74 i1f1 ItTl f1) ii 11 II 1 1 3 .0 14, 6)1,1 34 643 200 35 B 78 It 9.5 10,7 11 « T, 11 II 4 9. 5 it fi w n 1ST. P. 11 11 1 11 IT n 600 10 11 n 11 1 Tl 11 ii i SC Small Churn LC Large Chum BP Navy Fuel Oil Tetrachloride B Benzol GO Gas Oil .. -·'.---~_r~ • t~ ,~ t ~ >4- .5 6 1 s Y ~ ~.."... Pulverization Oil No. Raw Coal Approximate Gal.. Type of average Per Agl- Exp- Cor'ed Lab. diameter Ton tat- eri- Ash Ash Su Coal. Number Mesh of Kind io~ ments 'fo 'fo J ~1~ Particl.es ~ J Anthraoite Culm. 6....5 1u3' ~ Nn. 5(6) 27 7 3q,4:~·1 " SC , ft " It 1t T. .. , lJ " ttl 35 N. 62 s u n .. . I 11 " ~ II SC 1 u If 1 U 'It " u LC 2. u 1r .. " :" LC , u u " " 1t 11 SC II • " ft T. II SC u u " " N. F. 80 s , u Q ~ u n B 70 s 2: n '" 600 N.n S 4 t, lJ " , n U LC 2 1J u-n , B tJ SC 3 u t1 3 " " It 1.f tt II 1l u 62 " 31 • .5 34;9 , . " 62 u 4 u t, 9 N. F. 70 LC tT n u G. O. n u u R. I. Anthra.oite 78127 .550 N. F. n tt 1 21.7 23. 8 Wasb. Semi. II 76141 3.5 n 79 S , 12. 6 , 3. 9 .5.50 , , U II S , " " " , t If " LC n " Pittsburgh Bit. 78385 65 130 " t 2.3 14. 2. 1. " 130 N. F. " " , n ." '. B. " " " tt n 3.5 N. F. n SO 1l n 700 n 10t! J.,C " 1I s 4 , 2" .5 n 1 . " ft " C. T. " " 7 " n " u N. F. n " 4 " n 600 9 n " " , 13~' 0 14 6 1. 1 Upper Freeport 1t 1 ".5 1 J". 7 • II '1 C. T. n 4 ~ • .5 II It " N. F. t1 n " " 11 " " , n u 6 Shaker CT Carbon Tetraohloride Churn N'li' j- (' -, " 11 2 3 5 6 7 8 9 to 34 644 34 n it tt n « if n 3 6?74 120 « » n 200 55 n u 600 10 111. Bituminous 7 5$ 37 200 35 ti Tl H 200 35 ti tt tt 200 35 if n 1* 700 6 n 75637 130 ti « tt 100 80 n n M 200 35 it ti If 200 n n W 800 5 n If 3 In&, 7 6027 200 35 ti 1* ti 575 Tl w it 65 1I1t titi iitt 120000 3850 Eenn, Bituminous 75823 600 9 tt it 75540 9 Lla. ti 7 5581 600 65 9 3kla. H 75631 130 U tt 65 130 it it ii ti H ti 200 35 11 tl ii 200 35 tl • tl it 200 35 11 It ii 600 9 few Mex, 9 w 77538 600 /ash. Bit. Coking 7 61 42 65 130 it It T» ii 200 35 ti II 11 ii 35 it 11 It n 200 35 ti It 11 w 200 35 n If 11 it 700 6 tt If If n 6 /ash. » Hon * 6185 9 tt It If w tt B s 7 8 1 4 2 7.1 UF 11 if 2 tr If n 11 ti 1 n ft B sc w 1 8,0 n ft it ] If. it HF LC if ft tt B 1 10.5 12. 1 CT It it 1 TT t» IF 11 LC iitt ] m n it W * tSiC ti \ 17. 4 it 21,-7 If It is ti f. # 11 1111 ssc ttti ww IIft ini SsC n1 9 1 9*9 13If. 0 titiii 1SL1CC iiwti 111 n?* Iffftt n IT »t ^ IV ft ii LC 1 1 4 5 1 4 2 u u 11 1 13.1 14. 5 u it 80 1 4 9 8.3 it tt 1 1 9 .5 23.5 n SC ii 1 ii ii n sc ii 1 it w ft » 1 it it sc it 1 it it tt 11 TT | n tt II 11 1 n it UF 1 9. 4 10; 5 B SC 78 2 22, 6 24.7 « 11 2 n 11 n 1* n 1 tt ft s it 2 n 11 ittt ssc iut 22 titt I1f1 Tt LC tt 2 IT 11 11 s it 1 26,9 29.4 11 it it 11 2 3 4 5 6 7 8 , to I Upper Freeport 34644 200 34 .S 78 , 6.2 7. 1 ft. 1t " 300 34 :rifF " " " tf 11 ft lJ 600 10 " lJ " , u " " u 36?74 65 '20 H SC "' , 8.,0 9.9 . U 11 " 200 35 1f u U , " " ··t. " n n 600 '0 UF LC t,. 2 1:f: " t', 4 n.l.. 75\837 200 35 .Jj s 82 'O~ 5 12, $ ,t<' 11 II " 200 35 CT " If 1 n II ~:: n " " 200 35 11F 11 11 i :t't " ~' .,,\ " ., \t 700 6 n LC It 'i " .. ~ '-... -: ~. " " 75637 65 130 " SC 81 , , 7. 4- 21.7 '-_'J : .. .-~ " n n '00 00 n 11 n ., '\ n .- • " ' .... ~ It II n 35 11 TJ l1 't II t1 r .. ': .~'.t 11 U tr 2.00 35 II s u -I u u , :J " u u 800 5 u SC n ., n tt I " n It 900 3 u sa l' 1 ~ " Ind. Bituminous 76027 200 3.5 11 s 79 i G 9 1.3,0 11 " ., .57.5 10 " LC " , /t U n " n 65 130 11 SC n 1 " n 11 n '00 80 u 11 1l 1 'l " I £ n u If 200 3.5 u u " 1. n " r.e, nn. Bit um.inous 75825 600 " 78 1. 16.5 , 6. n 7.5:540 660 ' " n " 13~! 1 , 4, .5 -~ :' .. ll.a. n 75.581 600 '7 lJ U 80 , 6., 8, 3 '~ )kle.. " 75631 6.5 130 n S 11 , 19 • .5 23 • .5 II n " 65 130 u sa n , .. n n 100 80 II SC U "It "" " n " 200 35 " sc u , u: n ~.<, 11 U " 200 3.5 CT SC " n n .. ~~~II '. " .- n " 200 3.5 It u " 1 " ., " n n 600 'u n " ., n Cew Mex. n 1'7.538 600 , NF LC 51 1 9.4 10: .5 ~ash. Bit. Coking 76142 65 130 sc 22. 6 24. 7 " It .. " 200 3.5 " s " n " " .. " n 200 35 " ,. " " " 1t " n " 200 3.5 NF S n " " " .n " n " 200 35 " SC " 2 n " 1- •. n " 7(JO 6 n S n 2 n " ~ . It " 1l " 700 6 n n n " lash. " Non "' 7 618.5 600 " S n , 26.9 : " " " " " 600 9 n LC 1t 1 n " ,". ~ ~ t.). .::. , I'".· 1 2 4 5 6 7 8 9 10 , frazil Bituminous i 6025 200 NF 39.7 w 11 n 9 » 1 n Pgh.* Bit. Wash Ref. 7 8386 700 6 H } 2 48.5 [|h. Bituminous » w 6 U 74 1 w 'Fpper Freeport "bone 65 130 B 79 SC "I 2 1 .7 24, 0 ooal refuse n 35 11 11 sc w IT 11 n n 35 11 SC n M 11 n n 35 UF » sc w 11 11 ii 11 35 B 11 w 11 w M 35 CI 11 s 1 11 11 II n 11 35 Isl'F 11 s 11 11 II ii ti w s 11 ti w « n 11 1,1 11 II n 65 B 11 s 1,1 11 II n 200 35 11 fl s w W 'enn. Bit, Refuse. 77541 6 MF 50 LC 1 la. Bit. ¥/ash.» . 77 864 575 10 11 79 LC 23. 5 69. 26. 2 ew Mex, Bituminous 77559 25 n 61 } 54. •59. 3 Sub-Bituminous7 61 84 1,1 119 s 1 1 5 .1 4 9 ii n 575 10 n 11 \ 11 11 ii » 35 11 105 SC 1 11 1.1 J w n M 108 1 21. 1 ii 7 5897 II w sc 2 11 11 w it 11 w sc 2 11 11 n 11 »1 u sc 2 H 11 n 600 11 II 2 11 11 exas Lignite ,75823 200 35 n 100 s 1 20. 2 22. 8 w Carb. 500C. n 25 11 77 sc 1 34 9 al,, Lignite** .« 7 602 6 430 11 94 sc 1 39. 0 .Dakota . 200 35 11 98 s 2 8. 8 10, 1 ~ 3 i r I ~ra.zil. '7 9 I n " 11 600 ') ft ~gh; 78386 '400 n i)gh. .Bituminous tt " 200 1) irpper bone 34645 65' .coal " 200 " " u " CT n 11 n HF 11 n 11 n n 11 CT 11 11 lifF 11 " 600 9 " 11 11 600 9 n 11 6.5 130 tJ U n ann. Bit. 77.541 700 liF .la. Wash. " • 77864 " Mex. '77 539 300 25 11 ,ash. Hi tuminous7 65 130 u 11 " n nu lJ 200 " " 65 130 t,t 1J 75897 65 130 tJ n n 100 30 n 11 n 200 35 It n n 9 n ,7.5823 u " 500e. ft 300 " : B-1., Lign1 t elt .'" '76026 450 15 u , '~Dakota Lignite, , • 75472 t,t I , I , B 78 LC 1 78 LC 1 64 LC 1 LC 1 sc t 11 sa 1 l.l se t u SC 2 1J s 1 11 S 1 11 S 3 11 S 1 11 LC 1 It S 1 n S , , 1 LC 1 s 1 n LC , , '05 se 1 s 11 sa 2. It SC 11 SC u LC '00 S 1: sa SC 18 S 35. 6 " 43. " 21. 7 n n u T.I u lJ 11 1J '" U 63. 5 23 • .5 '7 15. 1 n " 19. 3 t1 U n " 33. 5 35. 1 8 1 ,', j f- 39. '7 lJ I 48. 3 f' tI ' 24,0, " u U U 11 lJ U U IT IT 6;1. 4 26. 2 3 1 6. :7 n u 21. 1 I n U , u I u 36. ') 01 10. , , l~~ .10 _'L.' ",,1., , TREUT AUD AflfD M TESTS. Coal Lab. Separation*- Raw Ash Ash Ash Culm 34 647 & S, 1, 6c 3 -30,2 3 -29.7 Trent R. I. 7 6127 F 1, 3 10 1 4 3 21.7 Wash. Bit, 61 41 F 1.70 3 -13, 6 6 Freeport 7 6974 F & S 3 - 9. 8 0 111, & 1/65 -4 2 8. 17. 4 Ind. » 7 6027 F 3 -Ihd. 7 6021 9.9 • F & 65' -18.1 Wash, " 1. 35 3 -10 30,1 n 3 -10 w Trent 1. 36 600 2 4 9 Wash. Sub-" 7 61 84 F 3 10 12. 2 15. 1 7 5337 F & "S 1.35 3 -10 20.9 600 19. 5 33. 2 32. 5 1 8. 2 23. 6 0 13.9 20. 6 2 1 .7 13. 0 13. 0 19. 6 23. 5 32. 8 32. 8 29. 4 13. 6 1 4 ? 22. 8 21. 1 1. 01 . 94 1. 00 1.17 . 85 . 58 • p 2. 60 2. 34 5. 88 5. 61 4. 49 4. 38 4. 11 4, 74 . 5? . 59 •6! . 56 1. 21 •4i . 48 32. 8 7 4 81, 0 82, 0 0 98.5 55. 83.0 83, 4 2 32..5 4 1 0 64 68. 0 5. 4 ?• 6 8.9 1 5 .7 4 7 4 5. .6 4 7 4. 4 4 3 1. 6 12. 5 8.2 10. 0 the float and sink method, employing a liquid of the density indicated. ~BLE IV .$,.,2P=4.#4+I\, .. tr'1..a4,,*¥+N +f:S H.! ¥¥4"'4!lJiff"*.,,~Q.; COMPARISON BETWEEN RESULTS OF TRENT PROCESS AND FLOAT AllfD S INK TES TS. \ _ .. ' ',:.,'" Coal Cleaned Coal Coal. Method of Mesh Corrected Ho, Separation@: Asl1 Sulfur Weight Anthracite 34647 F 1. 6(. 3-20 30 .. 2 33,2 1.01 n 1. 70 3-10 29. 7 32. .94 . Trent 600 27.7 30. 4 1. 00 It. Anthracite 76127 F & S 1. 60 3 -1 0 , 6. 3 1 1. 17 Trent 600 21.7 23.6 • 0" 5 Semi- .Bit, 7 6141 F & S 3-10 13. 6 15. • .5 8 Trent 600 12. 6 13. 9 • 55 Upper .1!'reeport " .. 76974 1. 36 3-10 9. (5 11. ') 2, 60 Trent 600 8, 0 9. 9 2. 34 Ill-. Bituminous 75637 F S 1. 35 65-100 1 6. .5. 88 Trent 200 17. 4 21. 7 .5. 61 n 76027 F & S 1. 35 3-10 9. 8 0 4. 49 'Ind. " 76621 Trent 600 2. <) 0 4, 38 Okla 11 75631 F S 1. 35 65-100 1 8. 1 19. 6 4. 11 Trent 200 19. 5 5 4.74 Wash. 11 761 85 F & S " 3.5 3 -, 0 3 o. 1 32.? • .51 Tr1e1 nt 1. 47 3-160uO 2"6 . 9 3229.. 4<:.l •• .6519 Sub-lt 76184 F & S " 36 3 -1 0 1 2. 1 3. 6 • () 6 Trent 600 1 5. 6. ') 1. 21 1t n 11 75337 F &r~s " 3.5 3 -, 0 20. 9 22. 8 • 42 Trent 690 19 . 5 • 48 A. F & S indicates that separation was carried out by li~id denSity indicated, .5. 58. 8 9. 6 76. 5 2.9 e'.0 15. 7 82. 0 6.7 72. 6. 6 91. 79. 0 4. 2 :1 8. 5 6.7 5.5. 6 4. 6 83. 0 7. 6 83. 6. 6 95. 6. 3 79. 8 4. 0 69. 0 5. 7 32 .. 0 7. 6 .56.1 12. 1 80. 0 1 2. .5 74. 5 8. 2 90. 8. 3 66, 0 7. 8 6CJ. 0 1 D. J .~ .. I,~j' , ,;i : ~ '. ·t·, . , I Ash Weight AS11 Ash 42,3 1. 26 41. 2 5 8 .3 63.7 1.51 23. 6 88. 9 4 5 1.33 1 9 .0 1 8 .8 20.7 . 70 1 8 .0 90.1 . 95 28.0 3 1 .5 . 48 9*0 84. 5 9 1 .3 ..0 30.8 3 7 .8 1 .5 87.6 97.5 4 3 0 ) 44. 4 30.7 37.7 8.59 17.0 65.1 7 5 . 1 0 . 10 1 6. 6 26,1 33.0 9. 21 4.8 86.2 9 4 6.70 20.2 61.1 7 0 .9 9.37 31.0 50.5 59.3 9.00 40.1 44.5 . 51 53.1 . 57 20.0 84. 2 ( 0 . 00) 25.5 26.4 1. 15 10.0 80.0 86,9 .90 34.0 4 6.3 50.2 . 29 1 2 .0 .31 Sulfur Reduc- -tioa. Combustible Recovery . 50 . 55 . 75 1 . 28 . 83 . 62 . 60 . 96 2.30 3. 71 4.26 3. 4.27 2.7 6 3. 08 . 60 69 •7 6 1.25 . . 50 £2,2 67. 6 67.8 3.7 69.1 5 1 . 5 53.9 5 7 .3 1 6,2 7 1 . 5 54.2 7 4 5 7 6 .8 59. $ 5 3 .5 32.8 45. 0 62.7 48.2 50.5 41.5 25.0 9 .4 4 9 13. 2 62.3 1.7 34.7 24.1 21, 6 2 .5 32.4 35.0 2 7 .1 1 . 7 1 6.0 1 1 . 3 . 3 -1 4.2 4 4 1 7 7 .8 98.8 8 1 .5 99.7 7 8 .4 85.2 99.9 65.2 87.2 98.3 92.7 85.8 44.5 7 2 ,3 9 7 .5 7 8. 2 99* 8 78,1 99*0 ~~- ._. ---"--.-. " Refuse Ash Sul.fu.r COlllbustible Corrected Reduc- S .50 67.2 42. } 46.4 1.26 82.2. .50 • .5 46.1 i~·l .55 41.2. 58.3 63.7 , • .51 41 • .5 77. B • '7 5 2-3. 6 138. 6 96 • .5 1.33 2.5. 0 1.28 11.0 18. 8 20. '7 .70 3.7 - 9.4 81 • .5 • B3 t 8. 0 90.7 98.5 .95 2.3 • 20.0 }1 • .5 34.3 .48 51 • .5 6.. 9 '78.4 • 60 9.0 84 • .5 91.3 (0.00) 53.9 -13.2 99.1 .. 96 21 •. .0 30. 8 37. 8 8.70 57.3 8.5.2 -I ,2.. 30 , • .5 87. 6 ')1.5 ( 6.30) , 6. 2. 1.1 3.71 44.4 30.7 57.1 8.59 71. 5 6.5.2 4.26 17. " 65. 1 75. 6 10.10 54 .. 2. 24.'1 94.7 \'3 58 1 6. 6 26.1 }3.0 9.21 34.1 21. f" • ;~ 4.27 4. 8 86.2. ') 6. 6 6. 70 36.4 2.5 '~, ,f, 23..078 6 3201..20. 5610.. 51 75~0.. 93 99..3070 7766,.58 3352.. 4() 9823..18 ;\ : 16 67.2 40 .. 1 44.5 .. .51 74. 6 - 27.1 44 • .5 43.9 .53 .. 1 57. 6 .. .57 .59. B - 1.7 72.3 . ffj 84.2. 90.9 l O. 00) .53.5 -16.0 97.5 .76 2.5 .. .5 23.9 2. 6.4 , • 1 5 1\. 6 ']8.2 1. 2.5 10.0 86,9 45. " - 3.3 9'7. 8 ,4 '.49 34. " 46.3 50. 2 .29 62. '7 -1 6.7 78. 1 • .50 12.0 86.5 86.5 .. 31 48.2. 4. ~ 99.0 ~' :~ ",. ... , t;,. ' , ~".' . II ! " I ': ..• . ~~';::"" :I':f~ ordinary 'float and sink' tests and Trent Process results is given, Mixtures of carbon tetrachloride and petroleum naptha were employed for solutions of density up to 1, 60 and sine chloride sol­ution for higher denisities. The results give an idea of coals. specific separtaion in general exception{ much Process, reduction float anth­racite, while Process ash reduc­tion per cent. Farther will course Sulfur Rfs&ov&l General Considerations; removal pyrite coal action slate, by par­ticularly sub-division Comparison with ordinarY washing methods: In table 4, a comparrison of results of f:Loa.t~ Erocess given. ~~tures an~ ~etroleum na~tha ~ployed 1. bO zino c~oride den1s1t~es" resul.ts g1ve what might be expected were ordinary washing methods applied to these coals, It will be seen that the spec11'ic gravity se~artaion gives general. as good ash and sulfur reduction as Trent Process treatment. Combustible recovery is, with one exception( the Oklahoma coal ), muoh higher by the Trent Prooess. Practically no ash reduotion was obtained in the fl..oat and sink test with the Rhode Island anth­raoite, whi1.6 Trent Prooess treatment gave an a.sh reduc-t ion of 69 :per oent. Further discussion of these tables wi~ be given in the oourse of the paper. Sul.+u.r Removal. General. ConSiderations: The removaL of :pyrite from ooal by any process depending on selective aotion of oils is considerably more difficult than the removal of other mineral matter such as shale or slate. Pyrite is readily wet oil and par­tiaularly wnen in a fine state of SUb-division tends to DISTRIBUTION FORES SULFUR, Uoal Oil Pyrit- Sul- Org- Ash di- ie phate an- in tion ie refu.se Illinois 115631 Raw R Indiana ?6027 R Jpper Raw ?reeport f 6974 Oklahoma [5631 R lefuse from (5 mthravite Raw Julm R I ($15 defuse £rom W15 IF nC T HF B 1 7 . 4 5. 6% , 57 2, 5 .6 8.0 7 .7 7 .4 3 , 66 4,94 4 . 46 5,28 1.96 1,88 2.09 , 02 .21 . 1 8 1. 68 2. 85 56 3. 01 44.9 62.1 69.9 9*9 4.38 4. 1.79 . 1 2 . 13 £. 86,2 8,0 7 .2 2,*1 1,96 1.44 1 . 36 .®5 . 02 . 58 1 .5 .9 4.74 3.75 3.01 2 , 10 . 36 . 1 5 1.37 1.50 46.3 6.50 4. 85 . 35 1.30 31.5 7 .0 1,74 , 85 1.21 .13 . Of .47 . 65 66,1 66,1 2.73 2,41 .01 .31 TABLE V DISTRIBUTIOli OF FORMS OF SULFUR. ~oal. Con- Mesh Ash Total Pyr1t- Sul.- d1- used 10 phat.e &n- t10n 10 refuse Il1.1no1s 17.4 5, 61 2.40 .. 57 64 '75637 200 NF .. 6 3. 66 , .. 96 ,02 1 .. ~8 44.~ " \1 CT 8. " 4 .. 94 ' .. BE .. 21 2 .. {)5 62.1 n u n 7.7 4.46 1. 65 .2.5 2. ;6 30.0 n n HF 7.4 .5.28 2.0'9 .. 18 3.01 69. ') Raw ' .. 9 4 .. 38 1 .. 79 .12 ~, 47 1 602.7 600 \1 b,3 4,. 27 1.37 • L5 2.79 8 .. 0 2.. ~1 .. 0.5 .. 72 freeport R 200 J3 7,2 1 .. ,6 .. 3 6 .. 02 .. 58 87.7 I tfJ74 Jklahoma 1.5 631 Raw 1'9 .. .5 4 .. 74 3 .. 01 .. ' .. 37 " CT -7 .. 9 3.7.5 .. 1 0 .. 1.5 1 .. .50 46 .. 3 iefuse trom r 5 631 CT 6 .. .50 4 .. 8.5 .35 , .. 30 ~nthra .. ite 31 • .5 ' .. 74 , , 2.1 .06 ,47 ;ulm " 7. " • 8.5 .. 1:3 .01 , 6.5 66.1 I {f)7.5 {eiuse ~rom i: 697.5 bb, .. 2 .. 7 3 2 .. 41 ,Ot ,31 ~' - ~ ~ ~: i !'I I I ! ,f ~ • ~ r l " Table 6 3oal Mesh Avg# Mie- Lab, dumber Raw Coal Recovered Coal Refuse Sulfur- gulffar iliuois 5 637 klanoma 75631 ndiana 6027 130 100 80 35 10 aoo 600 130 80 35 10 200 65 130 100 so 200 600 35 10 130 reeport 200 80 6^7 6 600 10 ittsburgh 65 130 8385 200 cO 600 10 nthracite 63 130 aim 200 4 647 600 10 900 3 ithracite 65 130 ilm 200 m 5 600 10 78183 78211 78185 78189 7 8181 78182 23 19, 47 8, 01 12, 30 27.70 31.51 5, 61 4.74 2.21 L75 7.55 5.91 5, 57 7.37 5.77 5.97 5. 68 4.30 9,.87 8,54 9. 04 6.29 7.90 7, 43 6.73 9. 40 9.70 6.20 1.00 12,80 8,00 6.00 5.20 1.74 13.70 6. 00 5. 00 4,2 6 3,95 3.66 4 28 3.46 3 . 17 3. 08 2. 64 4. 05 4, 24 4,0^ 4. 27 2. 09 2.34 1. 68 1. 69 .81 . . 71 n 1. 60 1.30 Ask 65.1 5 5 .6 44,9 69.7 57.7 52. 6 50,5 8-6,2 79. 89.5 7 8.0 82,0 89.0 70..0 72.0 Per cent sulfur reduction 24 6 33 35 44 8 3 7 5 4 30 8 EFFECT OF F I M E S 8 OF GRINDING 01 SULFUR REMOVAL Tabl.e 6 EF.b'ECT o If INE.l.~ES S GRINDI.NG Olli RElIil.O VAL ...... "" 80a1 Av~" .Lab. size l~umber R§w Coal. ,Eeco:y::ered Co~l R~i'use Mic- su1ful: rous Ash Sultur_ A~h Sulfur Ash reductie.,n llinois 65 130 72\83 17.41 5. 7 .. 55 4,2.6 65. 1 5637 BO 78184 3.95 55. 6 30 '-1. ..'0r.1. 5.57 3. 66 44.9 35 6uO 7.37 6. 2.8 69. '1 6 klahoma 65 781 8)1 19,4'1 4,74 57.7. 27 15631 100 ,80 7818\ 5.9'1 3. 1 '1 dOO 5.68 3.08 5·0.5 600 A-2.5 4.30 9 .. 87 4.38 8.54 4.05 602.7 10j 80 9.08 4.24 9.04 4. O~ - 6uo 6.29 4.27 6" 2 3 pper 65 130 8,01 2. 2.1 7.,)0 1.93 13 80 '1.43 2.09 - 6976 6,73 87.7 130 12.30 1.7.5 ~. 2.03 7~. 6 bO 1,68 80.7 6- 20 '. 69 B~ .. 5 3 n.thraci t e 65 130 2.7 .. 70 12 .. 8e • 81 78.0 19 Ll.lm 2:00 80 8.00 .. 70 82.0 30 ,4647 600 10, 6.00 .71 88.0 29 JOO 5.20 .70 8>,.0 I I ;l:thraci te 31 • .51 1,,74 13. '1 (j ' .. 60 70• • 0 11m 80 6.00 1 .. 30 25 b97.5 , 0 5.00 .. 0<) 88.0 49 itself coal-oil agglomerates than in Separation is coals. S;Utrib^t4Qfr fforms off SuUttX: in clearly in following analyses anthracite will tiere con in the recovered coal. In some cases it will be noted that the organic sulfur in the recovered coal is lower that in the raw coal. This does not mean tha the organic sulfur har actually been separated from carbonaceous material by the fine pulverization but that part of the carbonaceous material and combined organic sulfur has been discarded as refuse. Effect of Fineness of Grinding: In results pulverization attach itse~f to the coal-oi.~ agg~omerates rather remain suspended the water. Se~arationis accomplish­ed with greater ease from anthracite than from bituminous Distribution of Forms of Sult:Y.:t- This difference behavior of anthracite and bituminous coal is shown olearly the fo~lowing ana~yses showing the per cent of total sulfur, sulphate sulfur, pyritic sulfur, and organic sulfur in bituminous and anthraoite coals before and after treatment by the Trent Process. It wi~l be seen that in the case of the anthracite coal, the pyritic sulfur has almost disappeared from the recovered coal, while in the case of the bituminous coals t~e is still a oon siderable percentage of pyritic sulfur remaining ooal. organio reoovered ooa~ than ooal. arganic ha.r aotually by pa.rt carbonaoeous Effeot Filleneee table 6 the resul.ts of the treatment of several coals at different degrees of ~ulverization TABLE 7 Character Original Recovered f mixture Mesh Mixture Coal oal Coal Pyrite Ash Sulfur Wt. Ash s 80 100 17.89 9.72 J 1 , 4 12,70 5.61 ree- » 92,9 14,4? 7.41 »ort 200 4644 f 97.4 17.03 8. 44 ' 2 , 6 6?,42 f 3. 2 ',3 99,3 17. 1 3 ?.54 » 9^.8 17. 1 3 8,98 17, 2 4 9.47 w 97.5 1 6 , 1 5 8, 82 35.40 23. 21 87.5 28,7011.45 8 6,9 3 0. 3213. 41 8. 6 66.3 7 .1 23.8 14,5 6b.15 2. 13.2 .7 88, 68 1.9 0 1.2 86,70 7 .6 0 UO 85.51 2.6 0 82,13 9.3 50.7 12.5 13.1 82,7 2 7 5. 09 0 42, 2 0 Jpper 80 free-port ? 6974 20 200 19.33 10.91 96.5 1 7 . 7 1 0 . 1 0 3.5 9 L 3 15.1 8.95 8.7 7 9 , 70 7 8.93 1 8 ,0 5 [Hi- 80 1 0 is 58B7 20 200 600 2 1 . 35 10. 23 84.1 11, 88 ^ 9 2 15.9 85.2 12,34 7.11 14.8 7 0. 33 79. 63 42,1 50.5 14 0 jithra-w >ite julm 14,647 IT 100 200 35. 08 9.94 63.0 1 6,08 3.3 6 3 7 .0 60,2 10.72 1,39 39.8 69. 87 66.2 24 6975 "• 600 3 8 , 12 10.53 57.0 9.92 2. 82 43.0 77.26 73.2 2.5 600 35,0 , 3 6 2 . 3 6 4 5 . 0 77.90 77. 6 3.7 SYNTHETIC MIXTURES OF COAL AND PYRITE Refu.se f> & Sul- Oil f> fo in Wt. Ash Reduc- Ref-tion use TABLE 'Z. S YNTHET IC Refuse % % f m;Lxt~~ Coal Sul- Oil % fo 'fa 'fo % % % % % fur i:n 08.1 S Wt. Ash Reduc- Ref-tion use pper 20 ~.12 ·~1404 12.70 .5.61 f. 66 • .5 42.3 1 n 92..9 , 4. 47 7.41 7,1 66.98 :5 fort 200 8.5 • .5 10" 25 3. 89 14 • .5 66.'.5 60.0 1 ,4644 n 97. 4 17. () 3 8" 2" 6 69.42 , 3.2 .3 600 99.3 17.?3 9 • .54 • 7 SE. 1.9 " 9 0, b 1 7. 1.5 8. 9 8 '.2 86.70 7. 6 u 99.0 17.24 9.47 , ,.0 8.5 • .51 2. 6 u 97 ."3 6. 1.5 8. 2.7 82.13 9.3 0 50 50 100 2:1 87 • .5 28.701'.4.5 , 2 • .5 82.72 .50.7 " 600 6. '9 "30. 3 21 3. 41 13. 1 7.5. 09 42.2 1 O. '~1 96 • .5 17.7 10. ,,, 3.5 79.70 7.4 0 rree- 600 91.3 , .5. 1 8.9.5 8.7 78.93 18.0 3 ~ort 16274 ~olllei - 2.0 26.0000 21.35 10.23 88.45.,21. 1121,.3848 7;J,,1? 2t ' 1154..~8 7790., 3633 3420..15 '4 ,5887 " .nthra-" 3.5,08 9,94 63. 0 h4 DB 3. 3 6 37. 0 67. 67 66.2. 2:4 ~ite 2:00 60. 2: 10.72. 1.39 39. 8 69.87 86.0 40 IUlm L4~647 tf)75 " n 38,12: ,10,53 9 .. 92: 43. 0 73.2: 2.5 600 5.5,0 8 • .56 2.36 45,0 will bituminous pul­verization finer than mest is detrimental to the removal of sulfur. With the anthracite coals finer pulverization is not detrimental* and in one case better sulfur removal was obtained by treatment of the coal ground to about mesh than by treatment of the 200 mesh material. S vnthe tic ftiixtur e s o f Coal and Pyr i t e: pyrite remov­ed from a mixture in which the pyrite was known to be separated from the coal particles. The re­sults are set down in table Conclusions 10 practically removal pyrite has been finely ground with the coal. With subdivision (200 it was possible to get as high as 60 per cent re­duction erratic. example,$he which 60 per are set down. It wi~l be seen that sulfur removal is not large with the bitUlllinous coals and that pu1- verization 200 r~oval sulf~, tiner »u1verization detr~ental. r~oval ooal 600 meSh Smthetic ,ooJ-xtures of Coal. agd Pyrite; A study of synthetic mixtures of coal and pyri te was made with a view of determining defi­nitely the per cent of pyrite which might be remov­e d :pyrite partic~es. 7. Conc~usions from the results of treatment of synthetic mixtures of coal and pyrite as given in table 7 are as follows: 1. Mixtures of Upper Freeport bituminous coal and pyrite, containing about per cent total sul­fur, show praotioally no pyrite r~oval when the »yrite mixtures in coarser state of subdivir'ion (200 mesh), of sulfur altho the results are erratic, For exam»l.e, ~he mixture whioh gave a cent reduction in only 13 experiment, 2, A similar of Illinois showing sulfur reduction of 42 per cent on 200 mesh mat­erial and 31 per cent on 600 mesh material. 3, A culm a 86 200 a-bout 75 600 material, Ooal 46 alone iaery suspended in thv water. different removed Process, In general, little trouble amalgam, large Results pre-reduction one experiment, gave on~y per cent reduction on a duplicate expertment. 2. stmilar mixture o£ I~lino1s bituminous coal, Big Muddy, gave a recovered coal Showing mat­eria~ 31 600 3. A similar mixture of anthracite oul.m and pyrite gave & recovered coal showing a red­uction of per cent on mesh material and a­bout per cent on mesh material. Coal pyrite containing about per cent sulfur was used in the experiments. It was found possible to make an amalgam of the wet ground pyrite a~one with very little of the pyrite re­maining th" It is apparent that di£ferent coals very in the ease with which pyrite may be r~oved from them by the Trent Process. genera~, anthracites give very litt~e troub~e with pyrite being retained in the a.ma~am, while bituminous coals retain a ~arge amount of the pyrite even tho it has been physically separated from the coal by the pulver­ization. Resu~ts point to the desirability of pre- 1 iminary removal results exper­iments pyrite py­rite treatment by the Process. SYNTHETIC MIXTURES SHALE ATO GYPSUM In removal, deemedHadvisable a finer coal completly Trent Process. Obviously the results of the Trent Process treatment of coals at different degrees of pulverization are of fundamental importance if it is certain that all the mineral matter physical ly separated from the coal by the pulverization is removes, by the process. If this can be shown to be the case, conclusions oen be drawn as to the fineness of dissemination of the mineral matter throught out the coal substance and as the fine­ness of the particle of so-called intrinsic or in-l1minary concentration by ordinary washing methods for remova~ of pyrite. From the resu~ts of exper- .. iments with synthetic mixtures of ~yrite and coal, it has been shown that little data of importance can be obtained in regard to the fineness of py-ri te before pulverization and treatUlell~ 1Ji/ tile Trent Frocess. S YNTHET IC MUTURES OF COAL WITH AND GYPSUM. connection with the study of the effect of fineness of pulverization on ash remova~, it was deemed 1adviss:bl.e to determine whether a. fine~ ly ground mixture of coa~ and shale or gypsum with coal could be comp~etly separated by the ObvioUB~y resul.ts trea.tment pu~verization fundamenta~ ~portance physical­ly by pul.verization renove4 coa~ in- results in finely divided pyrite is not removed by the pro­cess. In seem. results lubricating oil( about 4000 seconds Saybolt vis­cosity at 2j? degreesC) was used as the agglom­erating agent. 4IIS AVAILABLE FOR THE PROCESS Practically any oil or other organic liq­uid employed that of mineral matter, Certian commercial emulsions herent ash. From the res~ts of experiments with synthetic mixtures of pyrite and coal, it has been shown that little importance can be obtained in regard to the fineness of pyrite coal, because no~ pro­cess, table 8 are set down results of experi­ments with mixtures of shale and gypsum with a bit­uminous coal from the Pittsburgh se~. Table nine gives such analyses as were available of the mat­erial used in these mixtures. Comparison of the resul~s of the Trent Process treatment of the raw coal alone and of the several mixtures will show that practically all the mineral natter added was removed by the process, except where the heavy lubrioating 25 degreese} ~ILS AVAIlABLE Praotically ot~er not miscible with water may be ~ployed in the Trent Process, Very viscous oils require t1;):at the water be heated in order to reduce their vis­cosity sufficiently for the efficient separation matter. coal with siiale gypsum. Composition Coal Shale or fo f> Oil Agita­tion. Sulftu too - EF 200 S 93.0 7.00 1.31 7 .0 84, 2 . Old 53.3 46.7 ?i n « 49,4 7..06 22 50. 6 92,8 1.05 - w 53.3 n w II 50.3 7.94 1.40 49.7 93.3 . 78 ~ ft 600 c 9 1 . 5.42 1.24 8.4 90.1 - Pgh, shaleBO 20 B n IT 73.3 5. 41 1,09 26,7 9 L 5 . 5 1 ; n UF it n 74,0 6.07 1.27 2 6. 0 91.9 - n CJ « Hvy ti n 74,1 6.75 1. 21 23.9 90.1 - lb. t» B n 75.0 5. 64 1.38 25.0 84,1 .95 n n 11 H3? H II 7 5 .3 5.34 1.14 83.8 - n n n Hvy it ii 7 6,0 6. 63 - 24. 0 - ~ Table 8 1 Synthetcc mixtures of Pittsburgh coa~ wi th shale and gypsum, .. r Kind of Type Com:Qosition Oil. Mesh of Recovered Coal Refuse mixture Used Agita- 'fo Gypsum ojo tion. Weight Ash Sulfur Weight Ash SU.l:f~l Raw Coal 1 CO NF 2:00 :93 .. 0 7 .. CO 1 .. 31 7. " 84.2 " 63 Ol.d Ben .53.3 " " 11 shale 49.4 7.,.06 1. .50, 6 92.8 1 .. 0.5 ' \1 ; 93,3 "' " n .50.3 , .. 40 49.7 93 .. 3 .78 Raw Coal 100 n C 91 .. 6 .5.42 ' .. 24 B.. 4 90. , ~ ;'Pgh. shalebO :B " n .5.41 LO' 26.7 9' • .5 .. .51 " 80 n NF n tl 74. " 6.0'l ,. 27 26 .. C ?1.9 11 d·.,) " It " 74.1 6..15 1. 21 2.5.9 ~O .. l Gypsum n " .B n 7.5. 0 .5. 1,32 2.5.0 84,1 .:1.5 '1 II NF 11 " 7.5.3 .5 .. 34 24.7 83. 8 " n " n n 76,0 24.0 82,2 lb. : ------ Shale Shale Coal Gypsum 1 , 73 2, 20 9 1 , 1 0 90,00 C02 , 82 3.90 Org. carbon . 39 - w .27 - H2O 5,64 3.90 S i 0 2 50.37 59.3 AI.O3 22. 1 8 .5 Fe20-5 1 2, 01 5 .3 1.90 MgO 2.06 1.6 so2 .03 ,9 S03 ,00 .2 2.30 2.9 1 2 , 33 12.33 gypsum ant in mixtures. Moisture Ash CO2 oarbon 1l nitrogen Table 9 Analyses of shale, gypsum. and coal Used synthetic mixtures .. Pitts-burgh 1" 7 8 91.10 .82 .39 • 2:.7 Old Ben Illinois 2,,Pitts­burgh Coa.l 1.53 12" of hydration 5 .. 64- Si02 Alc:03 45 Fe203 ' 2:. 01 CaO .3 2.06 S02 ,,00 , 2 K 2 0 ) ) NacO ) 74.38 and B.S. sucessfiilly. of the material must not be too great. following made with different oils and three coals, anth­racite culm, a bituminous coal from the Pittsburgh seem, and a coking coal from the state of Washing­ton, The liquids used vary in viscosity from that of gasoline to that of heavy topped Mexican crude which poured with difficulty at room temperature. Facilities were not available fro measuring vis­cosities higher than about 4000 seconds Saybolt so that the viscosity at room temperature of the three Mexican fuel oils is not known. liquids. reduction includ-ind which 40 temperature. wi£h oils obtained with an oil of 4000 seconds viscosity. The heavy Mexican oils running 455 seconds and upward ( at 65.3 degrees C) were used with the such as water gas tar and~.S. petroleum emulsion have been used sucessful1y. Here, again the vis­cosity The fo11owing table gives a series of tests 011s ooals, anth­raoite Pittsburgh. cok~ coal. lrom. Washing­ton. 1iqu1ds o~ neavy to~ped Mexioan orude whioh di£iioulty Faoilities uere viscusity lVlexican Results show that the best ash removal is obtained with the very this 11quids. Ash reduotion is about equal with the liquids up to and inolud­ind the gas oil whioh ran seconds Saybolt at room tem.perature. Beginning wi~h the light fuel oilS of 80 seconds and upward, ash reduction is not so good, altho very appreciable ash removal is viSCOSity. 435 65.5 C) . " Table Bit ,7 6142 Anthracite -7 697 5 viscosity Sec, Say't, 13.5C Grs, Deg, Coal Refuse 1000 Be. Sulfur Q u e * & J ft [Raw Coal) Darbon Benzol Carbon tetrachloride Gasoline ^erosine ias Oil ?uel Oil A fuel Oil B fuel Oil C lubricating Oil A * w * w b .exiean Fuel Oil A a w tt « B& it « n Qa ater .,S, Emulsion 80 250 57 1 800 150 4000 240 945 240 . . 825 1, 600 #72:0 . 800 .835 .83; 892 880 897 910 ?58 3% 54,2 37.7 29.1 27.0 2-9.1 26,1 23.8 6,1 1 5 .4 3 1 .5 5.9 6.5 6,5 6, 6 6, 4 8,0 8, 6 9.0 10.7 12. 1 14,0 8,5 9,.0 8, 4 9 .2 9 .5 1.27 1 . 2 3 -" 1.22 1,2 8 1. 38 1. 29 1.23 1,22 1.39 1.29 1.23 33 1.34 U 3 8 1.27 1,21 1, 28 ' •87.1 87.0 88,5 87.1 87.2 84,1 85.1 85.>0 84, 6 87.2 86,9 87.3 85.4 86,1 88,0 85,1 85.2 22, 6 1 6,0 6, 4 18,0 18,7 n 20,1 19. 0 1 8 ,9 20,7 1 9 .2 U . 0 18,7 1 8 ,8 18,9 Refuse 77, 0 7 4 .5 7 5 ,1 7 6,0 5 ,9 79.1 80,1 81,0 81.5 7 7 .4 7 7 , 78.3 7 9 .1 7 6 .4 viscosity 65.5 ASH REMOVAL WITH D^FERMT QIIS Tab~e 10 A.SH WITh Dli'J:!'EREJ.'fT OIrs Liquid used (Raw Oarbon disulphide benzol 90% ; arbon tetraohloride }asoline :erosine ~as ~uel l'uel 13 i'Uel ,ubrioating A 11: n C ~ n B .exioa.n Fuel 0il Aa n n 11 Ba u u ca at er Gas Tar '. S. Emulsion ~isoosity Density See. SaY't. '.5. ,5C GrSj Deg. 2.5C , ooe per be, Anth.raoite Culm 40 80 135 2.50 400 1800 4000 455 0.0. .• 825 1. 600 .7cO • bOO ,u~;7) 5 • 8.52 , 880 .57 • B92 .880 150.897 143 .:110 • ~ 58 240 .963 2.40 • '97" 76,75 Cleaned Coa~ Re~use Ash Su~fUr Ash 2k ~ % 31 .. 5 .5.9 39 .. 7 6,5 .54, 2 6 .. 5 64,4 6.4 45.0 6.6 37 .. 7 6.4 34,3 8 .. 0 2'9,1 8,6 27. () 9 .. 0 29.1 10,7 2: 6, 1 23, 8 14." 1 6. 1 8,. 5 15.4 2,0 14,3 B.4 9,2 9.5 '. 27 ,87, 1 , • 23"- 87, 0 1,22 88,5 1.28 87, 1 1 • 3 8 87,2 1.29 84,1 1.23 85. 1 1.22 85 .. 0 1,39 84,6 1, 2~ 87,2 1,23 86,9 1, 3~ 87.3 1,34 85.4 ' .. 38 86.1 , • 27 88.0 1.31 85,~ 1, 21 / 85,. 2 1.28 / Washington BlL 76142 Coal -Re:fu.se Ash Ash 'l:: % 22. -- 6,. 0 77.0 1 6,4 74.5 - la,O 75,1 , B,7 76,,, " 7 5.9 20. 1 79. 1 , 9 .. G) 80, 1 1 B, 9 81 .. 0 20,7 81, 5 19.2 77.4 1/ 0 .0 77 .. 5 , u,7 78.3 18. 8 79. 1 1 8. j 76,4 a Water heated to 80 degrees C., visoosity measured at 6.5 • .5 degrees C - and 100 degrees C. Table 11 raw Agita­tion in Amal­gam Gran­ules Re* cov-ery Ash Fuel B 13,2 20,3 35.0 5-6 9 6 2 I • 2 37.2 13,3 13,3 .1 4,0 96,0 97,0 93,0 10,8 10,1 9.7 .91 . 77 . 69 88,7 87.3 86, 0 oil C 24,5 36, 8 66 9^ 2,5 1 6, 3.0 97.0 92,0 11.1 11,2 ^69 75.7 85.5 Mex, fuel 26,7 46,5 117 , . 8 1.0 14,7 12, 3,0 94,0 96,0 10, 1 1 . 3 , 60 .97 80,5 84,3 Mex .fuel 34,8 47.0 37 117 3,0 2,0 6 13,3 . 5 4,0 98,0 13,5 14,2 :ll 88,4 M e x fuel a 21, 43,5 53 2,0 2,0 20,0 17,3 3 .0 99, 0 9 ,4 10,2 . 65 . 71 78, 84,2 a_ 80 C, Effect of Varying Amounts of Oil. Coal- 34647 Raw Coal - 27,7 1° 1,00 <fr Sulfur, Oil Used &ratB Qil"~ ft of Gal, Time Water Size Oil Recovered Coal Refuse ~a.b~e ~;fiect y"arYing Mounts 0:£ Qil. Coa~- Anthracite Culm 200 Mesh Raw 27.7 % ash, 1 • 00 % Sul.:fu.r, ui1 A.mt. Qi~ Analysis <fa 0:[ Gal. T~e % Water Size Oil Recovered Coal Re:fuse per of of Re~ Ash Sulfur A.sh coal ton Agi ta.- Amal- Gran- cov-tion gam ules ery mm • ~ - Fuel. oil 13 .. 2 36 37 .. 2 . , J6" 0 , O. 8 .~1 88.7 .5.6 ~ 13" 3 4.0 97" (j , 0, 1 .77 87,,3 3.5.0 '96 2 , 3. 3 ~3. 0 , (lJ 86" Fuel ert1 "~, 24, :2 66 3 , 6" '6 3,0 97.. " , 1, t 11 ~" ·1 ~5 .. 7 3'6, B 9' 2" .5 13.3 92" 0 11,,2 ,69 5, .5 Mex,,:fuel A 2. 6" 7 67 .• 8 14.7 3.0 94.0 , 0" 8 • 60 80" .5 46" .5 , , 7 1" 0 12. 6 96. " ",. ,~7 84" .5 .M.ex ,file], " B 87 3. " 26, .5 95.0 , 3 • .5 "17 88.4 "11 2:.0 13.3 4.0 98.0 , 4.2 • 2 86, 6 .M.ex fue~ C 2.1,. 6 53 20,,0 3.0 95.0 9,4 • 65 78" 6 A 43.5 108 2" 0 17.3 99.0 , o. 2 .71 84.2 A Water heated to degrees C. during agitation. gable Details Balance Coal Pittsourgh t. wt. Dry, Oil Wt. Wt. Of oil from extraction acta Uhae-frrs wt. Refuseoil Balance aExp. Amalg, RerVe ount in for ing drying wash 1:2:3: 4 : 5 ^ <?0 $ <& GrS, Crs. Amal."Refuse wa.tft-r, B n u M n it tt ii CT ii it « tt tt tt verage $5*5 BP w H tt tt tt H tt tt tt 47,7 IMF » tt ii n tt tt tt 81,5 85 42,5 266,3 27 6, 2 273,5 27 8. 5 273,5 2-73,5 27 8, 354,0 357,1 352, 354. 5 353.0 356,3 177,4 181, 177.2 175,4 20, 5 14,5 18,4 21,0 17.5 17, 18,3 6.5 17,5 - 295.5 1,4 295,5 n 2 88. 8 m*i 294, 6 294,5' 29 6, 0 2f 0, 5 2 9 1 ,8 1 9 , 5 2 1 . 2 6 1 9 , 9 2, 1 7 . 3,2 1 9 . 0 4. 0 1 7 . 1 4.8 10,0 8 6.3 S 1 1 . 4 tt 1 3 , 3 1, 1 2 . 2 1 # 6 295,5 ~>,5 ,4 11 n 11 1,1 2 H M tt W 190, dye, 6 375.1 379, V 5 7 5 ,5 375,4 37 6, 4 3 7 X ? 188,2 188,7 1 89, 4 1 89.9 1 89, 8 189.2 2,3 ,2 ,3 - ,2 1 .8 1,3 1,9 - .2 1 .0 1.4 ,4 1.3 1,3 1.1 - .4 .9 1.0 , 8 ,4 .2 . 2 . 5 85,1 2,2" 14,7 9 1 2,2 6, 8 91, 5, 2 3,0 9 5 , 9 U 4 4,7 94,5 1/8 3,7 89, 4 2, 0 8, 9 5 . 3 3.5 1,2 95,3 1. 2 3,5 85, 2 4, 0 1 0, 8 9 1 . 9 6, 1, 6 9 1 , 8 5, 4 2, 8 Tabl.e 12 Detai~s of Oil palance Sheet Coa~ used 200 mesh Fitts~gh bituminous. Distribution of oil' ·Coal wt. vit. wt. steam Mineral from extraction ~ t,a Dry Dry distilled matter Unac- Oil Used Amalg-Refuseoil carri- dissol- Ba.lanoe a ' ., ~. A.ma.l~.Ref.oount am, ed over dur ved loss ", fo~ Gr. Gre, Gre , Gre. Ainmagl .dEr-y~ifnugse . wwaasthe r. 1 :4:.% % % % ~9 5 • .5 :B 81 • .5 266.3 20.5 295. 5 288 .. 8 2.3 u n 277,4 14 .. 5 '" 4 295,3 2-"_' 2.1,. u 276,2 , B. 4 u 294 .. 6 .. 2 " 273 .. .5 21.0 II 2,4,,5 .. 3 " u 278, .5 17" 5 1, ) u 2,6 .. 0 -,2 " , .59 272,7 17. 6 u 2"",} 1,8 11 u " 273, 5 18, .3 1I 2'511, S 1,,3 " 203 .. .5 1 6. 5 II 290, Q , .. 9 IvI erage ~, 278. . 5 17. 5 H 229.Q ~ '"9 5,5 nN F B5 354, " 19.5 1. 6 32'8950 .,. 5.5 327,25 ... 16 1t.. 4<J 8.5,,' 2, -2. 14. ~ 11 l~ 3.57. 1 21.2 1. 6 n 37'7,> ' .1 '9' , 0 2, 2 6. . .. . II lJ 352. 6 19, ~ t!., 6 .4 1. 1 " 37.5 • .5 1,.3 ~1, 8 5.2 3,0 n 354,5 17. 3 3 .. I::. 11 19 375. . 4 1. 3 9.5 .. ''I 1,,4 4.7 " 11 n 3.53.0 19.0 4, (} U 1.1 376,4 L 1 ~4 • .5 1 ",3,7 35 b,.3 17,1 4,8 lJ tl verage 51'i; 2;; 89.4 2,0 B, 6 47.7 l'lF 42 • .5 10.0 • .3 8v. 5 " 11 1 Bl .. 6 6 • .3 1 Jv .. ,88,2 1" 0 9.5.3 3 • .5 1. 2 n 1, " 177.2: ".4 1nt n 175.0 13,31 n.. 6 Iut 11 88-89..74 •.. 48 ~8 55..32 4' ... 02 130 •. .85 " 17.5.4 12,2 1. 6 0 n 189 .. '9,2 '91. ~ 6,.6 '.6 ,4 lJ 82. 8--f. 91 .. 0 .5 .. 2. 190 .. 2 , 89, 2. • 5 tMs similar viscosity room temperature. In the case of the anthracite coal, it will be noticed that less combustible matter is thrown out with the refuse as the viscosity of the agglomerating oil increases. JLEOOTT OF OIL USED In amount # 5 lb. per pound of dry cleaned coal. If the coal contains 25 per cent of removable be about 62 gallons of a light fuel oil per ton of raw coal treated. With coal ground to pass a 200 mesh screen, this quantity of oil produces an am­algam in granules about 1/8 inch in diameter. If finer ground coal is employed, it may be necessary to use as much as , 4 pound of oil per pound of dry cleaned coal to give an amalgam consisting of the same size granules. 11 using culm a 200 screen. necessary form amalgam in granules about 1/8 inch in diameter varies from coal water heated to about 50 degrees C. Worked at tAis temperature they give ash reduction comparable with that obtained with an oil of stmilar visoosity at ooal, notioed refUse agg1omorating inoreases. AMOUNT 0 n .. much of our work oil has been used in an azount equal to .3 lb, per pound of dry cleaned ooal. ooal ~5 r~ovable refuse, it will -oe necessary to use 450 pounds or 200 s'creen, llroduces 1/8 as.qluoh .4 llound of oil per pound of dry "', Table 1l shows results of a series of tests uSing different amounts of several oils in treating a sample of anthracite cu1m ground to pass e 200 mesh soreen. The oil neoessary to fo~ an amalgrua 20 per cent of the weight of the raw ooal in the measurement experiment. In a agreement between results of different experiments and to give proof of our conclusions that the unaccount­ed for loss of oil is that oil which it was not possible to extract from the amalgam. The first series of results give data obtained when benzol and carbon tetrachloride were used as an agglomerat­ing agent. It was possible to distill these liquids completely from the amalgam and refuse and these experiments therefore give data which serve as a nblank" for the subsequent experiments in which Navy Fuel Oil was employed and extraction necessary for removal of the oil. It will be noticed that these experiments show an experimental loss of about 1 per cent. Part of this is due to mineral matter disolved from the caol by the water, and the remainder, loss ox coal during manipulation. If this figure, i.e., weight of moisture free coal plus moisture-free refuse obtained in the benzol and carbon tetrachloride experiments be subtracted from and measur~ent of water and steam distilled oil: extraction of amalgam and refuse; distillation to dryness of all water used in the exper~ent. the following table e. series of data have been set down to show the agre~ent obtainable our- whioh -~ \ tetraohloride distill liquidS re~se exper~ents ~ bl.ank" for the subsequent experiments ruld 1 tne cao1by remainde~, 10ss o~ coa~ i,e 8 , in tetrach10ride fr~ the corresponding average in the experiments with Mavy Oil { o±" distilled amalgam refuse), result experiment, oummar- ized calculations Oil Calculated 6,9 - 2f2, = 84,3 83,0 1 89. 4(292, 6) t 42, 42,5 Anthraoite 177.0 - 143,7 = 3 5 , 5 34.0 17,7.3 - 143,7 ^ 33, 6 33,4 3 65,4 - 2(143,7) - 78. 0 76,5 3 5 6 , 2 - 2(143,7) = 68, 8 68,0 t h e s e s e e n t h at unaccounted ex­traction loss extraction amalgam re­fuse. Since t h e con­siderably material cleaned coal smaller suffici­ent accuracy which extractable the refuse. JBTo losses due to emulsif ication have Navy Fuel Oi1 ( weight 01' the amalgam plus oil ~istilled over during the drying of ama1gam and refusej, the resu1t should give the original amount of oil used in the ex~er~ent. Summar­ized caloulations from the table follow: Pittsburgh Coal. o il Calgu.lat ed 37 6" ,~ 292. 6 :;: 84,. 3 18'~,. 2 - i{2~2,. 6, ~ 42,.9 AJlthracite Coal. Oil Actually Used 8.5,0 42,. .5 34.0 33.4 76" .5 68,. 0 From thep19 calculations it is seen th~tt the UIU:.coounted for oil as determined from '8X-traction is not an actual lOBS but is due to incompleteness of extraotion of amal.gam or re­~ se. Sinoe the refuse in most cases is a con-s iderably smaller weight of matel'ial than the oleaned ooal and contains a smalle~ percentage of oil, the oil loss may be taken with suffioi­ent aocuraoy as that oil whioh is extraotable from No ~ulsifioation - finely emulsification.In - In experimental separated bulk by In cases oil results, cleaned correction oil re­maining in amalgam. factors in ( 1 ) carbon­aceous contained, 2) Physical charact­er can coal increased combustible in no direct relation between amount of combustible matter and oil absorbed can be shown for all coals. In our experience the refuse from anthracite coals have been the worst offenders in absorbing oils, consisting practically been found, ~ Apparently the presence of fine~y divided coal prevents ~u~sifioation.rn setting ~ regular exper~ental procedure, the refuse is separa*ed from the bu1k of the water fil­tration. several oases the water was decanted and distilled for emulsified oi~ with negative results,. down data fro per cent ash in c~eaned coal in extracted amalgams, it is obviously necessary to make oorrection for the amount of oi~ re-maining iu. the amalgam • . Two faotors effect the loss of oil by absorption the refuse: (1~ Amount of oarbon­aoeous material oontained, (2; Physioal charaot­er of refuse. Thus, while it oan be said for any one ooa~ that inoreased oombustible matter the refuse makes for increased absorption of oil, oombustible oan coa~s. anthraoite oils. A refuse conSisting of pure shale absorbs practioally no oil providing a great excess of xoil $Z-$$ ash free When drops oil in the refuse is to be expected and an inc­reasing of the refuse increases. to which the coal is ground before treatment. For example, the refuse obtained by treatment of a bituminous coal from the Pittsburgh seam, pulv­erized to pass a 65-mesh screen, analyzed per cent ash, at 200 mesh 88 per cent ash, and at 600 mesh, 89.5 per cent ash; a refuse from Washington sub-bituminous coal analyzed at 65-mesh, 30 per cent ash, at 200 mesh, and at 6Q0..jaesh, 86 per cent ash. Evidently the clean coal and mineral matter are well separated at 65 mesh in the Pit­tsburgh coal while much finer pulverization is necessary to secure clean separation in the case of the sub-bituminous coal. --Illil has not been added in making the amalgam. Such a refuse, consisting for example of Pitts­burgh shale, might analyze 92-93 per cent a~h on the moisture-free basis. the ash content dXQPs to 84 per cent and lower, absorption of ino­reasing amount of oil is lost as the carbon content The amount of carbon in the refuse depends upon the character of the coal and upon the fine­ness b5-86 vent sub-bi~inous anal~~ed b5-50 600 mesh, ooal, The following table gives data showing oil number fihe oil used in these experi­ments Havy Fael in free free In "Condition", dry" amalgam; " indicates that coal in estimated observation column "Agitation, electrically Platettt. capacity 1300 "Shaker" carried 1-g- losses occuring in treatment of a num.ber of coals by the Trent Process. ~he oil used in these experi­ments was the Asphalt base ~avy Fuel oil previously described. 300-gramn samples of coal were used all the experiments. The amount of oil used has been figured in per cent of the moisture-free raw coal and in gallons per ton of moisture-free raw coal. the column llConditton", the term "dryl' indicates that the coal has been ground to pass the mesh indicated and agitated with water for a few minutes before the addition of oil and formation of the amalgam: 11 soaked" indicates the. t the coal has been ground dry to the mesh indicated and soaked water for one week before carrying out the experiment: "wet ground" indicates that the coal has been ground with an equal weight of water. Meshes finer than 200 have been estima;.ed from microscopic obaervation as subsequently described. In the coilumn nAgi tation, Type", the churn referred to is the el.ectrically stirred churn shown in Pl.ate,". wit a capac~ty of about 1500 cc of water. One part coal and four parts water were used in all experiments. nShaker" indicates that agutation was oarried out in ,~~ liter wide mouth bottles, set on LATA QE 1 Coal 2 4 5 6 7 Type Length ?&ofRaw Gal. f Refuse t o H o u r s Coal T o n , 600 a c 25,7 7 0, 2 36.7 s c ,7 22, 62,2 31, 8 11 s s 1,0 w ii 2 2 . 8 11 d s tt w 11 2 8 ,4 « c c 1,0 11 11 29. 6 » s w H 1 7 , 4 d s tt 11 tt u 26. 8 w d s w tt 26. 8 tt s s H w tt 2 2 . 6 d s tt tt 28.1 II s s w tt H 2 5 ,4 600 s 2 , 0 25,7 7 9 ,? 23,8 tt « s 11 tt 2 4 , 7 tt w c » w 62,2 25.5 tt tt c 1.0 w 70.2 23,8 tt tt c « w 7 P ,2 2 4 , 4 tt tt c m tt tt 23.2 tt tt c u tt 11 2 4 , 1 11 s s ,5 11 11 30.3 W Wg s 4 , 0 25.8 7 0 , 4 29, 8 t! M c 4 , 0 tt tt 2 % 2 IT tt c tt w 32,4 tt tt H s ,7 tt 11 30,3 s 1.0 w 3, 6 wg c 2 , 0 w IT 5.7 tt s , -/ tt 11 « wg c 4 , 5 28,9 11 23,2 « wg 6 ,5 2 8, c 7 8. 6 20, 0 c 23,3 63, 6 39,0 wg s 1,0 27,2 7 4 ,3 4 1 , 6 a s 1.0 23.0 62.8 59.2 « s 1,0 23.0 62.8 tt s 1.0 28.8 To. 6 59.7 6,7 Weight Ash $ gft, 11 Anth, Culm 34 647 6975 Wash-S,A« "Bit. 7 6t 83 Fit. 78386 J.Freeport Hutch Ref. J,Freeport 77, 6 81,9 ®,7 7 8 ,6 79.2 7 5 ,7 78.8 7 6.4 82,0 78. 6 82, 6 9 J . 0 89.9 89.1 8b. 2 88, 6 89,0 88.9 82,7 82,9 88, 6 P£ 0 88^9 p, 8 85,3 84,5 78,3 '84, 2 77,1 87.2 69,3 68,7 7 9 ,5 21,0 10,0 1 4 , 0 12,0 1 2 ,0 1 1 , 0 1 1 , 0 1 1 , 0 10.0 9.5 6,9 7 .5 7 ,7 2,2 1, 0 0 0 1,0 1 1 , 0 6,0 5,0 1.0 1,0 1 2 ,2 4 , 0 0 5,0 0 18,0 \>5 6,9 9,1 10,0 70.0 86,1 86,0 85,1 84,4 21, 6 87,1 87.1 90,1 88,3 92,3 93,1 92, 6 9 7 .5 99,1 100, 0 100,0 99,1 "87,0 93,1 94,4 98,7 98,8 98,6 99,5 100,0 96.0 69.9 97,7 82,2 7 6,4 97,7 Coal. Anth. 34647 7 6')75 S ~lJ .• .!::lit. 7618.5 it. .Free!,ort .TABLE 13 DETAILED DATA ON OIL LOSSES. 3 4, I Agitation Mesh Cond. Type Length %ofRaw Gal. 60G 200 n u n It n n tt n n n " u It 11 n u n " n n 200 600 600 n u 200 600 200 n n d s s d d s s wg It U U ,"". s wg " n nn d tw, g wg d d n n C C S S C S S S S S S S S C C C C C S. S C C S S C S C (J C S S S S Hours Ton, , • .5 .7 ' ..., 0 c:: ,/ , • (l " 11 n 11 u 2,0 n '. n () u tJ • .5 4,0 4,0 ,7 .7 '2 .., 00 ";! ,./ 4 • .5 . ,.5 c:: ./ 1. 0 '., 0 '. 0 '., 0 25.7 22. 8 u It n u n n u n n 25.7 n u II 11 I, n 1l 25,8 u n n " l.t 289 ~ , 2 lJ, C 23. ;: 27 .. 2 23 .. 0 23 .. 0 70,2 n u n n II n 11 U u 70, ? II 62,2 70,2 7P.? n " t1 7 0.4 n 11 n 78, 6 n n It 8 CJ _ Refuse vVe igh "CA.Sh %% Oil % '·1 Oil Recovery Table 13 contd. 1 2 3 4 5 6 , 7 8 9 10 1t J . F . 3 4 645 Jena, 77 541 .la. 77 864 77559 lash. 7 61 84 >ex 75823 ex *' & gh. 34 b67 • f. 34 643 1 1 . 75887 1 75637 ad. 76027 ad . " 31U1.75835 La. 75681 da 75631 -M. 77558 ish.7 6142 200 600 600 « 600 « 600 65 600 200 600 200 it it it tl II 11 200 200 11 ti d 65 d d d 11 n it it it it it it 600 wg 600 200 d 600 wg 200 & d 200 d 600 wg 600 63 a 600 wg 200 d 200 d 600 wg 600 wg S s s c c c c s G s c c s c s s s s s s c s s s c s G s s s c c s c s s s 1 .0 1 .5 1.0 2,0 1.0 2. 0 5*3.0 5:S . 8 1 .5 2, 0 3.0 2, 0 1.0 1.0 1.0 1.0 . 5 1.0 1,0 1.0 1.0 8 . 0 1. 0 n 4.,0 1.5 5.0 2 .5 1.0 1.5 .3 . 3 28, 8 7 8 #6 " A 7 4 6 8.4 30,2 28,8 78,6 22. 2 60, 6 43. 6 1 1 2 ,0 , 1 1 9 .0 108,1 » it w 3 6. 6 t 00,0 2 8 , 3 25.7 28,7 28,7 28,7 29.0 7 7 .3 7 8,3 it 2 8 , 7 2 8 , 7 30.0 7 9 .2 11 11 78.4 it 8w1 .9 3 8 . 1 29. 8 81,4 2^,0 1 9 2 29.. .0 79.2 28.7 29.2 29.4 1 8 ,5 28,7 11 79.7 80,3 50.3 78,4 78.4 78.4 78,4 1 1 . 9 1 1 . 8 1 .5 55.4 3.8 10.3 13.7 1 3 ,0 1 2 .0 3.1 20, 7.2 7.1 7.7 6.8 8, 4, 0 7 ,8 8.1 1.1 2 .5 5,0 8„0 1 1 , 1 7 .3 4.8 9.2 4, 0 1.2 1 1 . 5 1 1 , 8 92,8 7P. 6 80.0 85, 86,3 7 2 ,9 94.2 79. 3 84,5 85. 87.3 86,0 89.1 90.0 89,4 87.4 90.5 7 2 ,8 65.5 87. 86,2 89. 53. 6 86, 6 26. 7 7 .0 83.9 85.2 2, 0 2,0 1.8 12,4 3.4 5.0 0 0 1 .5 13,9 14,1 15. 20,7 6.4 9.9 10. c 15.0 2, 6 2 .§ 1 1 . 0 0 . 5 0 12. 6 25,0 . 8 12,0 1 6,0 3,0 4.0 1 00, 0 82,2 7 6.4 97.7 99.2 1 00, 0 1 9 5 ,5 99,2 98.3 1 00, 0 1 00, 0 9% 98,9 ?6,7 9 6.7 95.7 98.8 9 7 ,2 9 7 .2 ?9.4 99, 6 s 100,0 0 99.9 100.0 85.5 1 00. 0 100,0 2 3 4 6 8 10 1t I.F. 34 64.5 d S '. 0 28.8 78, 6.7 81.3 10,0 96,0 wg s , • .5 » " 11.·~ 87,0 2" 0 '00, t' ft S '.0 " 78,6 11.8 88,0 6~. 9.' ~enn. 7'1.541 ft C 2 .. 0 1 8,4 .50,2. 69.0 82,7 0 97.7 .1.a. 77864- 600 C ,. 0 28• 8 78.6 1:9 .. 5 22.8 0 82 .. 2 r.M. 77539 6{)0 u C 2.0 22.2 .55. 4 80. 6 1, 8 76.4 lash.7 61 84 c 5,...0 43,. 119,0 3. 8 7 Ii. , 2, 4 97.7 600 wg s 3. (j n 11·2 .. 0 , c. 3 97" 7 It 75897 c 5. 0 39. 6 108,1 , 3. 7 62,9- 95'.2 600 wg S • 8 ft " 13 .. " 85. 6 99,2 n C .. 8 " tt , 2. 0 86.3 100 .. " ~ex 75823 d C , .. .5 36. 100 0 3,1 72 9 2, 1 100" 0 28.3 77:3 •• ex 1l §. 600 wg S 2.0 20. 6 94,2 • .5 95 • .5 'gh. 34067 200 C 3 .. 0 25 .. 7 78,3 7,2 79,3 13.9 98.9 n n S 2" () 28" 7 n 7 .. 1 85.4 14, 1 92.2 n It S , .. v 28" 7 u 7 .. 7 84 • .5 15, 6 98" 3 n u S 1. u 26,7 n 6. 8 84,1 20.7 100,0 II " S 1. 0 79.2 4.7 8.5. 8 , 00 .. 0 U S " 0 II n 8,1 9. ') 99. 8 n n S .. 5 u u 8. 0 86 .. 0 , 0. 0 98 q 1. 0 'f ··ft n C 11 " 4.0 85.1 1 5. 0 '} 6,7 s " 0 " t., 7. 8 89, , 2. 6 96.7 wg S 1.0 It n 8,1 9'" 0 2. § '} 5.7 1, J 2 n '7 F. 34643 S o. , 1. 1 80.0 11.0 95 .. 1 C ' .. (1 ... r· 8 '1 It 2, .5 89.4 0 9 8.8 2.0 l~ * t 1.1.. ·75887 d S 30,0 81 .. 9 5~ 0 .5 97,2 600 wg (1 10,0 30 .. (} " 8 c 90 .. .5 " 97 .. 2 8.0 38 .. 7. 105. 6 ... 200 d S , 1, 4 72. 8 12,. 6 97.9 S 1.0 29 .. 8 81 4 17.3 63, .5 2.5.0 9?,4 rr tld. S • I 29.0 79:2 3.2 87 .. 6 8 99.4 4,.• a,d. s 29 .. 0 4,8 86 .. 2 C 99. 6 ',5 , snn. 7 5835 wg C 78.4 9,2 84. 6 • j 100,0 La. 75 68t 600 wg c 5 .. 0 2'9.2 79 .. 7 4. (} 89, 6 .0 9'9. ') rla 65 d s 2, .5 80.3 27.2 53, ,77538 600 wg c 1.0 8.5 50 3 5. 7 86 .. 4 <GI 96,3 1,. 0 .. / 1S11. 200 d S 28.7 78: 4 2,8 26,. 6 21,0 85 • .5 200 d S , • .5 " 78, 4 1. 2 77, 0 , 6.0 99.9 7, 600 wg S .:.;.. n '1 .. 3 83 " ~.- 3.0 100.0 600 wg c .. ;; II 78 .. 4 11. 8 8.5 .. 2 Plata: 11, One part coal parts refuse of moisture-free to the dry refuse plus oil. The value for "Oil" is value of the ash is per cent of the extracted oil-free refuse. Inspection tahle 13 will In necessary in most cases to grind the coal wet to meshes as fine as 600. Refuses from 200 mesh anth­racite culm varied in ash content from 7 6 to 84 per cent and contained 7 to 14 per cent oil. Refuses from 200-mesh bituminous coals analyzed 7 0 to 83 per cent ash and contained 10 to 13 per cent oil. Where parallel tests with the two methods of ag­itation were made, little difference in oil loss was noted. Refuse from the finer wet ground anth­racite coal contained 88 to 90 Per cent ash and from 2 to 8 per cent oil when agitation was carri­ed out in bottles on the shaking machine, and a shaking machine as shown in Pla.tt 1'. One part coal to three ~arts water was used in these experiments. The weight of the re~use is given in per­cent o~ the original moisture-~ree coal, and refers re:tuse :plus in per cent of the dry refuse plus oil, while the in oil­free refuse, Inspeotion of table will. show that none of the refuses which analyzed 88 per cent ash and upward contained large amounts of oil. order to obtain refuses of such high ash content it was ca.ses anth­raci te 76 a.na.lilzed 70 85 aE4 15 oil, dif:terence anth­raoite ooal per 2 out in bottles on the shaking machine, and 87-89 Per oil uniformily ab­sorbed oil. importance of separation. loss 1 600 dryj and treated by the Trent after merely mixing with water, shows a refuse contain­ing 77, 6 per cent ash and an oil loss of 30 per cent, & while the sme coal after soaking for six days, gave a refuse containing 82,7 per cent - such In the case of the bone coal refuse and Wash­ington contained from 81-8~ per cent ash and about 1 per cent oi~ when agitation was carried out in the churn. Refuses from bituminous coals similarly pulverized analyzed from 80 to 93 per cent ash and contained uniformi~y low percentages of ab-sorbed oil.. The following table gives data showing the ~portance o£ thorough wetting of the coal before carrying out the Trent Process separation, The coal which was wet ground to 600 mesh shows a refuse analyzing 88,4 per cent ash and an oil loas of per cent, the coal ground to mesh ( dry) and treated by the Trent :Process after contain-ing T1, b :per ~ While :per ~ This refuse contained suvh a quantity of oil that it was practically free from moisture when separated from the wash water, ash and an oil loss of 13 per cent. Less differ­ence is seen in the case of the 200 mesh coal. In the case of the bone coal refuse and Wash-ington bituminous coal, considerable less ash Table importance Condition Coal Cleaned Coal Refuse 3ul- Ash fur Ash Sulfur °fo <fo <fc fo fo <fo Anthracite 600 27,7 00 7,7 ,71 88,4 1 culm 34 647 27,7 1.00 7 , 6 77.6 3(3 dty grounft 27,7 1. 00 7,7 #? 2 but soaked 6 days be­fore treat­ment, 200 27,7 1,00 11,6 19,2 16 27,7 1.00 1,1,1 ,70 / 14 soaked 6 days 600 mesh 21,7 ,93 12, 2 ,75 88, 0 34 645 21,7 1 7 . 3 6?,4 6 days Washington 600 mesh 22,',49 13, 6 ,50 85,2 1,1 wet ground 7 6142 600 22,6 ,49 21,8 ,4£ dry ground soaked 6 days 14 Im:portance of thorough wetting. Coal Raw Coa~ C leaned Oil Loss Su1- A,sh Ash % % 'to 'to 8t4 'to Anthra.cite bOO mesh 21,7 1,0(.) ,.71 , . wet ground 34647 600 mesh ',00 7, 6 ,71 7'1, 6 3° dry '/ grounA 600 mesh 1 .. dry ground 7,7 , '92 82,7 13 be-fore treat-ment, mesh 27,.7 1, GO , ~, 6 ,72 79,2 1 6 dry ground ditto, 1,. 00 t"" .. 70 81, 9 14 soa.ked Bone Coal 60G ,93 l2,2 88,0 ,5 refuse wet ground 3464.5 600 mesh 2',7 ,93 17,3 ,87 6~, 2 4 dry ground soaked da.ys WaShington 22, .(6 , 49 , 3, b 8.5,2 , .. 1 bituminous 76'42 6(;0 mesh 22, 6 ,. 49 211, 8 ,4.5 coal coal. importance subjecting Process with . other in table 11 seem to show a some what lower oil be kept to a minimum. Our results have been obtained on a labratory scale and may not be translatable to large scale conditions but they at any rate point to the necessity for considering the question of oil losses in the refuse in any commercial installation of the Trent Process. was removed by treatment of the ooal dry ground and soaked in water than by treatment of wet ground ooal. The data point to the ~portanoe of having the particles of coal and mineral matter thoroughly wet before sU-bjecting the material to the Trent Prooess and indicates that wet grinding is the most efficient method of securing this desired condition when it is desired to pulverize finer than 200 mesh. Sufficient work has not been done with"­other oils to determine the variation of oil losses with the character of the oil. Results " loss in the refuse with the heavier oils. From the data obtained it is evident that the wet grinding to meshes finer than 200 is extreemely desirable if oil losses are to ~in~. oonditions poin~ oonsidering ~estion oommeroial 1/8 inch cent which hygroscopic coal. The content per cent prolong-er kneading. In granules, content 30 occurs coal particles, time In figure amalgam smaler is more finely pulverized. The lignite and sub-biyuminous moisture and hence do not fall on the curve. Method of Agitation Amount of Water in the Amalgam An amalgam in granules 118 inoh or larger usually retains 8-12 per oent moisture whioh will not drain out of the mixture, - in addition to the hygrosoopio moisture of the ooal. 'The water oontent has been reduced to as low as 5 ~er oent by prolong­er kneading, an amalgam of very fine granul.es, the moisture oontent may be as high as 50 per cent, A large part of this moisture oocurs as a coating of the small particles. The size of the granule depends upon the amount of oil used, the size of the ooal partioles, the method of agitation and t~e of agitation and to some extent on the cha­racter of the coal. table 15 and gigure 1 the relation be­tween size of granules and per cent water retained in the ama.lgam is shown. A sma.ler granule is ob­tained with a given amount of oil when the coal sub­biyuminous amalgams contain more hygroscopic fallon aurve. Brisk agitation of the kind given by rapid- Table 13 of and amalgam, Kind of Gals, Kind Lengtl Oil • D e r t o *v IF 70 C 2 IF 62 S 1 IF 62 S 1 B 79 S 1 tt S 1 CT tt S 2 IF tt s 11 u s 2 t* t* s 1 tt tt s 1 tt tt s 1 B 78 s 1 w s 1 IF ft s 1 IIBFF tttttt sss 111 If. tt s 1 tt ft c 1 B 82 s 1 CT tt s 1 IF tt s 1 n tt c 2 n 106 s 10,0 w s 4 i» tt c ,7 fi c 4 tt tt c 2 tt tt s 5 n c B 78 ft s 1. IF s 1 n tt s 1 ,5 rt ft c ,3 tt 79 s 4.5 tt n c . 5 it it c B 7 4 79 c s 1 tt s IF tt s tt tt s 1 .5 n c , 5 Per of ****** mfm I F n tt tt « v tt tt tt tt 50 79 62 IP 119 10B 100 ^ 8 120 C c c s c s s s s 2 1 5 3 5 1,5 1,5 2 50 13 25 12 12,7 7 V 9 9,3 1 P ,0 - 1 9 ,3 31,8 16,3 10,0 1 5 .0 30,0 24,0 13, 0 3 6,0 40,0 30.0 1 7 .0 17,0 45,0 22,0 3 1 ,0 2 6,0 49 50 16 65 21 15 28 34 34 30 34 20 36 26 25 50 53 37 27,4 30, 4 23,5 54.3 32,0 24.0 .1 5 2 2 2 6 20 12 6 1 2 1 2 .3 ,2 ,4 , 5 1 / 1 ' . 25 . 05 , 25 .1 2 6 1 ,2 .3 . 1 5 , 1 5 , 2 5 5 # 4 4 3 2 12 , 25 '5 Relation between size granules Coal Mesh Oil. R. I.Anth. 600 J?enne. ... Z-OO 34. 647' 600 . 1?ittsburghaOO Bi tuminous ... ... n" ... 400 600 Upper Free~OO port 34645 l' ./.ll,: 600 ... 34644 200 200 600 ... 76974 600 111.75887 200 200 200 600 " 75637 200 Ind~ 7 6027 200 600 Tenn75825 600 ... 77540 600 Okla7.5 631 65 N;?M. 77538 600 Wash76142 200 200 600 600 II 7 6, 85 600 ... ... 600 arazil 600 E?gh.7 8386 600 ... 34645 200 200 200 600 600 HF NF NF B CT NF " "... ... B CT NF NF B NF ~ ... B .N.. F n II n .".. n 11 E NF 11 " " n " n B CT NF II ... Per cent water in amal~ Amount Oil Gals. per ton. .7.. 9 ... " 11 ft " lJ 1l " tt tt " 11 " ... ... ... 79 " 78 n " 51 .7.. 8 11 ... .7.. 9 " '/4 .7.. 9 " II n Agitation Length S S S S S S S S S S S S S S S S S C S S S C S s C C C S C S S S C s C C C S S S S C 2, 3 t 1 t 1 ,,t t • 10. " 4 ~7 4 .5 2~ .5 • .5 .3 4 • .5 • .5 5 Eer Cent Water Size granules mm. paddle in work as previously described, oil coal and water were shaken in a stoppered bottle on a shaking machine. This method of agitation was first em­ployed because it gave conditions of agitation which could not be duplicated for a series of tests and premitted of quantitative treatment of mater­ials. It was soon found, however, that better ash reduction was obtained by agitation in a glass churn (Plate III) with paddle blades revolving at about 1000 r,p,mt and that certian coals which did not from an amalgam when shaken in the bottle were readily worked in the churn. In agitation and with two churns is shown. Table with clean water, was taken for analysis immediately after ^56- mation. The remainder of the amalgam was agitated with fresh water as indicated and another sample ly revolving ~addle blades is most efficient separating mineral matter from coal and in securing rapid formation of amalgam. At the beginning of our ~or -better p.m. in the following table a comparison of results obtained with the shaking method of 17 shows the effect of repeated washing of am­algams In these experiments a sample of amalgam ~ediately ~­mation. ~he Table 16 Agitation Raw Raw Per ash Per ash Per Cent Sulfur Coal Mesh Oil Coal Coal Cleaned Coal in Refuse Cleaned Coal Ash . Sulfur, a sc I£ § S£ i<c g sc LC. 34647 65 UF 27,7 1,00 1 1 , 5 75.7 ,81 65 12, 8 200 UF 12,0 ?,0 1 1 , 5 79.3 81,0 80,0 ,85 .70 200 11.6 5,7 8,4 85,8 76,3 78.3 .77 ,67 .71 7 6141 7 5637 6027 7 6142 11 It I 61 65 54t6t 45 « II 55897 KF 9,7 7,5 8,9 90.0 83,1 , 60 .65 .75 600 6, 88, 0 00 B 3,2 89.O .70 - 200 HP 1 2 , 6 ,33 1 1 . 0 5.8 75,8 , 52 600 1? 1 7 . 4 5, 61 84,3 , 57 200 11 8,4 7,4 & l 69,7 5 . 15 5.28 it tt 9,9 4,38 7. 9,0 4.20 4, 09 n 1 9 . 5 4,74 8, 8 5.8 53,7 83 3,46 200 tt 22, , 49 21. 0 18,7 77.0 65,0 , 52 , 43 t» CT 21,0 6,0 »•« 77,0 85.2 , 52 , 55 , 50 MF 14,7 83,9 11 11 26,9 ,61 12, 1 12,5 , 71 H 21.7 ,93 19, 6 17,2 71,0 69,0 , 96 , 90 200 11 1 8, 0 1 6,1 79,0 80,0 , 95 11 18,3 13,1 81,0 70,0 96 1. 00 n 8 .3 71.0 88,0 1,1 . 95 HF 12.9 1 2 ,2 87,0 . 77 63 19. 3 ,48 12, 1 2 ,1 51.2 , 53 50 <3Q . 75 S Shaker SC Small Churn LC Large Churn Ra.w Ia-ble 1 R Methods of Agitatio~ Ra.w cent Coal. Coal. Coa,l. 34641 bV0 7, 6141 ~ vO 6(,;)0 7.5 637 2(')0 7 602'1 n 75631 65 76142 n l' " 600 1 6, 65 \1 )464.5 65 It 200 n II It n " 600 5 5 8~n 65 A~b. Sulty.r S NF 27.7 1.00 CT NF B NF B J:) NF '2, 6 ,53 n n 17.4 5,. 6i 1.' ~ '9 4,38 / ,. n 1'91 • .5 4,74 lt 22,. 6 .. eT NF n 26, ? , 61 " 2'\,7 ,'J3 II B CT NF NF 19.3 .. 48 S C 18,5 , 2.0 11 ~ 6 ry,,7 n . .j 8.4 8,4 7 .. 6 8, G 21,. 0 14,7 12. , 9. b i b" 0 i 8 .. 5 1 8. 5 12,. :9 12,. 6 SC 1& 11, .5 12,8 9,0 11,5 8.4 7, .5 8" 6_ 0 5,2 I:; 8 /. 7,4 :J, 0 5 .. u<) , 8,7 1 6,0 13, 6 i 2, 5 17.2 , 6,1 13. 'I 14, 8 12,2 , 2, "j cent Sul.fu.r _ :a'efuse in Cl.e~ed CQa.l s sa LC S SC LO 75,7 , 81 77,7 79,3 8l. (1 ,. 85 ,. 76 8.5.8 16.3 18,3 ,,77 , 67 .. 71 ~O. 0 0.5. t 88, 6 " 60 , 6.5 .. 75 88, " ,71 89.0 ,70 75, 8 ,52 83,3 84, .5 57 .. 60 65. 5 69,. 7 5. 1 5 5" 28 87, 6 4" 09 .5.3 .. 7 57.7 3. 3.46 77. (1 65. (j " 52 .. 43 ~3" 4: 77.0 ,,52 ,. 50 83 g 85,. 2 • 55 • " , 78,3 84,2 ,71 .99