NOVEL GRINDING MIXTURE AND PROCESS FOR PREPARING A SLURRY THEREFROM

Abstract: A novel grinding mixture useful for preparing a solid-liquid slurry. This grinding mixture contains from 60 to 82 volume percent of carbonaceous material (such as coal and/or coke), from 18 to 40 volume percent of carrier liquid (such as water and/or oil), and from 0.01 to 4.0 weight percent of dispersing agent. The grinding mixture has a pH of from 7 to 12. There are at least two consists in the grinding mixture. From about 2 to about 50 weight percent of the particles in the grinding mixture have a median particle size of from 0.50 to 40 microns, and from about 50 to about 98 weight percent of the particles in the grinding mixture have a particle size in excess of 40 microns. There is also provided a process for preparing a liquid-solid slurry wherein the grinding mixture is ground until a slurry is produced whose particle size distribution is in accordance with a specified "CPFT" formula.

Description: DESCRIPTION NOVEL GRINDING MIXTURE AND PROCESS FOR PREPARING A SLURRY THEREFROM Technical Field A novel grinding mixture which can be used to prepare a stable, low viscosity slurry is disclosed. Also disclosed is a process of grinding said grinding mixture to produce said slurry. Background Art The prior art teaches that high density coal-water slurries have high viscosities and are substantially unpumpable. Thus, U .S. patent 4,104,035 teaches that a coal-water slurry which contains in excess of 50 weight percent of solids is unpumpable. Brief Description of the Drawings The present invention wi fl be more'fully understood by reference to the following detailed description thereof , when read in conj unction with the attached drawings, wherein like reference numerals refer to like elements and wherein: Figure I is a chart showing the correlation between the zeta potential of coal particles in a fluid and the specific conductance of the fluid as a function of percent dispersing agent added to the fluid for two candidate dispersants. Figure 2 is a flow sheet of a preferred grinding process for preparing the stable slurry described in this specification. D isclosure of Invention The novel grinding mixture of this invention can be used to produce a slurry which, preferably, has both static and dynamic stability as well as being pumpable at a relatively high solids content. This grinding mixture contains from 60 to 82 parts by volume of carbonaceous material , f rom 18 to 40 parts by volume of carrier liquid, and f rom 0.01 to 4.0 parts QMPI ^ NATIO of dispersing agent(by weight of dry carbonaceous materiaO.The pH of the grinding mixture is from 5 to 12. The grinding mixture can be provided either prior to or during grinding. In one embodiment, the carbonaceous material, carrier liquid, and dispersant are mixed to provide the grinding mixture, and the mixture so provided is then ground to produce a slurry. The materials can be mixed by means well known to those skilled in the art, such as blending them together, grinding them together, and combinations of blending and grinding them together. In another embodiment, all of the carbonaceous material desired in the grinding mixture is mixed with less than all of the carrier liquid and/or dispersant desired in the grinding mixture, and the incomplete mixture is then ground while the remainder of the carrier liquid and/or the dispersant is added during grinding; in this embodiment, the grinding mixture is generated during the grinding. In yet another embodiment, less than all of the carbonaceous material desired in the grinding mixture is mixed with carrier liquid and dispersant, and the incomplete mixture is thhen ground while the remainder of the carbonaceous material is added during grinding. As . used in this specification, the terms "mixed" and "mixing" refer to the steps of combining or blending several masses into one mass and include blending, grinding, milling, and all other steps by which two or more masses are brought into contact with each other and combined to some extent. Conventional means for mixing viscous materials can be used in this invention. The grinding mixture contains at least one carbonaceous solid material. As used in this specification, the term "carbonaceous" refers to a carbon-containing material such as coal, coke, graphite, char, and the like. It is preferred that the carbaonaceous material be a fuel such as, e.g., coal. Thus, anthracite, semi-anthracite, medium and high- volatile bituminous, sub-bituminous, and lignite coals may be used in this invention. In one preferred embodiment, the carbonaceous solid material is coke. Thus, e.g., one can use high temperature coke(which contains from 0.6 to 1.4 weight percent of volatile matter and has an apparent specific gravity of from 0.8 to 0.99), low temperature coke, medium temperature coke, pitch coke(which has about I percent of volatile matter and contains less than 0.5 percent of sulfur), and petroleum coke. There are at least two types of petroleum coke: delayed coke, and fluid coke. Delayed coke generally contains from about about 8 to about 18 weight percent of volatile matter, has a grindability index of from 40 to 60, and has a true density of from 1.28 to 1.42 grams per milli liter. Fluid coke generally contains from 3.7 to 7.0 weight percent of volatile matter, has a grindability index of from 20 to 30, and has a true density of f rom 1.5 to 1.6 grams per mi llil iter. It is preferred that the grinding mixture of this invention contain at least two consists of carbonaceous material. As used in this case, and in the prior art , the term "consist" means the particle size distribution of the solid phase of the carbonaceous material/fluid slurry. For example , in the prior art , the term "8 mesh x 0" , when used with reference to a coal-water slurry, indicated coal w ith a graded size, or consist , of coal particles distributed in the range of 8 mesh and zero, or 2360 microns x zero microns. Unless otherwise stated in this specification , the weight of carbonaceous material is on a moisture-f ree or "dry basis". Carbonaceous material is considered to be "moisture-free" or "dry" after it has been air dried by being exposed to air at a temperature of at least 70 degrees Fahrenheit and a relative humidity of less than 50 percent for at least 24 hours. In a preferred embodiment of this invention , at least two consists of carbonaceous material are mixed with carrier fluid to prepare the grinding mixture. Both of said consists can be produced by wet grinding; thus, one of the consists can be produced by grindng coal at a high solids content(60-82 volume percent) in the presence of water and, optional ly, surfactant, the second of the consists can be produced by grinding coal at a lower solids content(30-60 volume percent) in a ball mi l l or a stirred bal l mill , and the first and second coal consists can be ground together with each other(and, optionally, with one or more additional consists produced by wet and/or dry grinding) at a solids content of from 60 to 82 volume percent in the optional presence of from 0.01 to 4.0 weight percent of dispersant , and water. Alternatively, both of said consists of carbonaceous material can be produced by dry grinding; thus, one of the consists can be prepared by grinding one pulverized coal(i.e., coal which has been milled to a consist of about 20 mesh by 0) in , e.g., a ring roller mill , a second or more of the consists can be prepared by 5 dry grinding a second pulverized coal in, e.g., a micronizer fluid energy (jet) mill , and the two ground dry fractions are then blended in a blending tank at a solids concentration of from 60 to 82 volume percent with water and, optionally, 0.01 to 4.0 weight percent of dispersant at a high shear stress in a mixer such as a Greerco in-line mixer. 10 Alternatively, at least one of said consists can be produced by wet grindnig and at least one of said consists can be produced by dry grinding; thus, one of the consists can be produced by wet grinding coal at a low solids content(30-60 volume percent) in the presence of water and, optionally, dispersant , a second of the consists can be produced by 15 dry grinding coal in either a micronizer fluid energy mill or a ring roller mill , and the consists produced by wet and dry grinding are then blended in a blending tank at a solids concentration of 60-82 volume percent t with water and, optionally, 0.01 to 4.0 weight percent of dispersant at ja high shear stress in a mixer such as a Greerco in-line mixer. 20 Alternatively, one can prepare the grinding mixture of this invention by wet grinding(or regrinding) slurry comprised of carbonaceous material to produce the fine consist for the mixture. Thus, a fine consist can be prepared by regrinding a slurry at concentration of 40-60 weight percent soljds(and preferably 45-55%) in a stirred ball mill until the median 25 particle size of the carbonaceous particles in the slurry is from 4 to 20 microns. The coarse consist can be produced by dry crushϊng(in , e.g., a roll crusher, a gyratory crusher, a cage mi ll , etc.) the carbonaceous material to a nominal 3/8" x 0 size so that the median particle size of the coarse fraction exceeds 40 microns. The coarse and fine fractions then • 30 can be combined with each other, carrier liquid, and dispersing agent to produce a grinding mixture comprised of from 60 to 82 volume percent of carbonaceous material , from 18 to 40 volume percent of carrier liquid, and from 0.01 to 4.0 weioght percent of dispersing agent. The fine consist can alternatively be made by regrinding a dry pulverized coal at a concentration of from 40-60 weight percent solids until the median particle size of the fine consist is from 4 to 20 microns. QMPI styy f . WIPO O The aforementioned processes are all illustrated in Figure 2. The solid carbonaceous material in the grinding mixture of this invention consists essential ly of at least one fine solid carbonaceous material and at least one coarse solid carbonaceous material. From 2 to 50 weight percent of the solid carbonaceous material in the grinding m ixture is comprised of f ine solid carbonaceous material with a median particle size of from 0.5-40 microns. It is preferred that from 4 to 40 weight percent of the sol id carbonaceous material in the grinding mixture be comprised of fine solid carbonaceous material with a median particle size of from I to 30 microns, and it is more preferred that f rom 6 to 30 weight percent of said solid carbonaceous material be comprised of fine solid carbonaceous material w ith a median particle size of from 2 to 20 microns. From 50 to 98 weight percent of the solid carbonaceous material in the grinding mixture is comprised of coarse solid carbonaceous material with a median particle size greater than 40 microns. It is preferred that the grinding mixture contain from 60 to 96 weight percent of said coarse solid carbonaceous material , and it is more preff erred that the grinding mixture contain from 70 to 94 weight percent of said coarse solid carbonaceous material. The carbonaceous sol id is preferably mixed with from 0.01 to 4.0 weight percent(based upon dry weight of carbonaceous solid) of dispersing agent to produce said grinding mixture. In the case where at least two consists of carbonaceous solid material are mixed with l iquid , (l)both of the consists can be dry ground and mixed with liquid and dispersant ; (2)the dispersant can be mixed with the l iquid, and the dry ground consists can be mixed w ith the liquid-dispersant mixture; (3)one of the consists can be dry ground, a second of the consists can be wet ground with part or all of the dispersant , and the ground consists can be mixed with the balance of l iquid and dispersant which was not theretofore mixed with the consists; or (4)some or all of the dispersant can be wet ground with one or both of the consists, and the ground consists can then be mixed with the liquid and the balance of the dispersant which was not theretofore mixed with the consists; (5)one or more consists can be wet ground with no dispersant and insufficient total water and then blended w ith dispersant and the balance of the water and/or other consist blends. ATIO The grinding mixture contains from 60 to 82 volume percent of one or more carbonaceous solid materials. It is preferred that the grinding mixture contain from 64 to 81 volume percent of said carbonaceous solid material , and it is more preferred that it contain from 75 to 80 volume percent of said carbonaceous solid material. The grinding mixture has a pH of from 5-12. It is preferred that the pH of the grinding mixture be from 7 to II. The grinding mixture contains one or more carrier liquids. By way of illustration and not limitation, come of the liquids which can be used include water; aromatic and aliphatic alcohols containing 1 — 10 carbon atoms(such as methanol, ethanol, propanol , butanol , phenol , and mixtures thereof); pine oil; petroleum liquid(such as number 2 fuel oil, number 4 fuel oil , number 6 fuel oil , gasoline, naphtha, and mixtures thereof); hydrocarbon solvents(such as benzene, toluene, xylene, kerosene, and derivatives thereof); and the like. In one preferred embodiment, the liquid used is carier water. As used in this specification, the term "carrier water" means the bulk of free water dispersed between the carbonaceous, particles and contiguous to the bound layers on the particles, and it is to be distinguished from "bound water". he term "bound water" means water retained in the "bound water layer", as defined and illustrated in Kirk-Othmer, Encyclopedia of Chemical Technology, 2d Edition, Vol. 22, pages 90-97(at p. 91). The term "bound water" also includes water contained within the pure structure of discrete particles. Mixtures of at least two liquids can be used in the grinding mixture. Thus, one can use mixtures of water and ethanol, water and petroleum liquid, and the like. In one preferred embodiment, the carrier liquid is comprised of I to 15 volume percent of alcohol and 85 to 99 volume percent of water. In another preferred embodiment, the carrier liquid is comprised of at least about 90 weight percent of water and less than about 10 weight percent of petroleum liquid. In this aspect, it is preferred that the petroleum liquid be selected from the group consisting of naphtha, high gas oil, low gas oil, catalytic cracked recycle oil, mixtures thereof, and other similar petroleum products. Vegetable oils, such as corn, bean, or pine oil , may also be used to replace part or all of the petroleum liquid. The grinding mixture is comprised of from 18-40 volume percent of one or more carrier liquids. It is preferred that the grinding mixture contain r . V-MVIΓI - vripo ^NATI from 19 to 36 volume percent of one or more carrier liquids and, more preferably, from 20 to 25 volume percent of one or more carrier liquids. In one preferred embodiment, the grinding mixture contains from 0.01 to 4.0 weight percent of dispersing agent, based on the weight of dry carbonaceous solid material. It is preferred to use that dispersing agent(s) which is most effective for a given grinding mixture. Means for determining the identity and maount of the most effective dispersing agent for a given mixture will be described below for a coal-water mixture, it being understood that the method can be used with other mixtures. For any given system, the identity of effective dispersants can be determined by measuring the effects of the dispersant upon the system at a given dispersant concentration; viscosity at constant shear rate of the stirred coal-water slurry is measured while titrating with increasing amounts of the dispersing agent, and the point at which the slurry viscosity ceases to decrease is noted. For any given dispersant(s), and system , the most effective concentration is the one which gives the minimum viscosity under a given set of test conditions, and the efficiency of different dispersants can be ' compared by testing them with a given system under comparable cncentration and test conditions. Thus, one can dry grind a sample of coal in a laboratory size ball mill with porcelain or steel balls in water at 50 weight percent solids for 24 hours or until all of the particles in the coal are less than 10 microns in size. Small samples(about 500 milliliters each) of the system can then be deflocculated by adding various dispersing agents to the samples dry or preferably in solution dropwise, blending the mixture at any consistent blending energy(which may be gentle as mixing by hand, or at very high shear energy which will improve dispersion), and then measuring the viscosity at some constant shear rate by, e.g., using a Brookfield RVT viscometer at 100 revolutions per minute. The dispersing agent(or combination of dispersing agents) which is found to produce the lowest viscosity for the system at a given shear rate and dispersing agent concentration is the most effective for those conditions. Figure I illustrates a comparison of two surfactants for a given system. The curves of Figure I represent data obtained using both a purported nonionic polymer CW-ll(made by the Diamond Shamrock Process Chemicals Co.) and an anionic lignosulfonate Polyfon-F(made by Westvaco, Inc.) adsorbed on an Australian coal. The fine coal ground to about 100% finer than 10 microns is slurried in distilled water at 0.01 weight percent solids. Aliquots are placed in test tubes and increasing amounts of candidate surfactant are added to each test tube. The test tube samples are thoroughly mixed and inserted into a sampler carousel. The Pen Kem System 3000 Electrophoretic Mobility Analyzer automatically and sequentially samples each test tube and measures the electrophoretic mobility of the coal particles and the specific conductance of the carrier liquid; pH can also be measured on each sample. In Figure I , the left ordinate gives the calculated zeta potential of the particles in millivolts, the right ordinate gives the specific conductance in micromhos per square meter of the carrier liquid. These variables are both measured as a function of the percent addition of each surfactant on a dry coal basis, which is plotted on the abscissa. Figure I shows that the purported nonionic CW-il surfactant does have some anionic character. CW-II has a zeta potential of -50 millivolts at 300% addition on 0.01% dry coal. Polyfon-F has a zeta potential of -55 millivolts at 200% addition on 0.01% coal. These data establish Polyfon-F as a relatively more chemically effective, surfactant for use on this particular coal. ,. In general , from ) about 0.01 to about 4.0 weight percent of the dispersing agent is present in the grinding mixture. It is preferred that the grinding mixture contain from 0.03-1.8 weight percent of dispersing agent, and it is more preferred that it contain from 0.05 to 1.4 weight percent of dispersing agent. The dispersing agent can be inorganic; thus, e.g., one can use sodium hydroxide. The dispersing agent preferably is organic(it contains carbon) , and most preferably is an anionic organic surfactant. In one preferred embodiment, the surfactant is anionic and organic, and its solubilizing group(s) is selected from the group consisting of a carboxylate group, a sulfonate group, a sulfate group, a phosphate group, and mixtures thereof. By way of illustration, one of these preferred surfactants is a polyacrylate. Some of the surfactants sold by the Diamond Shamrock Chemical Company of Morristown, New Jersey can be used in the grinding mixture. Thus, one can use surfactants such as "Lomar D"(the sodium salt of a condensed mono naphthalene sulfonic acid) , Lomar PWA(ammonia salt of a condensed mono naphthalene sulfonic acid) , Nopcosperse VFG(condensed alkyl naphthalene sulfonate) , and Nopcosperse VEO(polymerized alkyl naphthalene sulfonate). O PΓ V ^VATlO Another preferred class of surfactants is the lignosulfonates. These lignosuifonates have an equivalent weight of from about 100 to about 350, contain from about 2 to about 60 phenyl propane units(and, preferably, from about 3 to about 50 phenyl propane units) , and are made up of cross- linked polyaromatic chains. In one embodiment , the dispersing agent(s) used in the system is a polyelectrolyte which, preferably , is organic. As used in this specificat ion , the term "polyelectrolyte" indicates a pol ymer which can be changed into a molecule with a number of electrical charges along its length. It is preferred that the polyelectrolyte have at least one site on each recurring structural unit which , when the polyelectrolyte is in aqueous solution, provides electrical charge; and it is more preferred that the polyelectrolyte have at least two such sites per recurring structural unit. In a preferred embodiment, said sites comprise ionizable groups selected from the group consisting of ionizable carboxylate, sulfonate, sulfate, and phosphate groups. Suitable polyelectrolytes include, e.g., the alkali metal and ammonium salts of polycarboxylic acids such as, for instance, polyacrylic 'ac d; the sodium salt or the ammonium salt of cndensed naphthalene sulfonic acid; polyacrylamide; and the like. In one preferred embodiment , the grinding mixture also contains from 0.05-4.0 weight percent(and preferably from 0.05-2.0 weight percent) of an inorganic electrolyte. Some suitable inorganic electrolytes include the ammonia or alkali metal salts of hexametaphosphates, pyrophosphates, sulfates, carbonates, hydroxides, and halides. Sodium hydroxide and/or ammonium hydroxide can be used. The grinding mixture can be produced by a process comprising the steps of (l)preparing a slurry without fines which cont ains from about 40 to about 60 weight percent of solid carbonaceous material ; (2)grinding the slurry to a fine grind until the median particle size of the carbonaceous particles in the slurry is from 0.5 to 40 microns; (3)crushing dry coal until at le.ast 98 wei ght percent of its particles are smaller than 50 mesh (300 microns) , provided that the median particle size of the crushed coal exceeds about 40 microns; and (4)blending the ground slurry and the crushed coal in specified proportions, together with dispersant. In the first step of this process, a carbonaceous slurry comprised of from about 40 to about 70volume percent of soid carbonaceous material and from about 60 to about 30 volume percent of carrier liquid is prepared; it is preferred that the slurry contain from 35 to 65 percent of carbonaceous solid material and from 65 to 35 volume percent of carrier liquid. In the second step of the process, the slurry from step one is fine ground in a fine grinder until the median particle size of its particles is from 0.5 to 40 microns and, preferably, from I to 30 microns. It is most preferred to fine grind the slurry until the median particle size of its particles of solid ca'rbonaceous material is from 2 to 20 microns. in the third stage of the process, dry carbonaceous material is separately ground until its median particle size exceeds 40 microns and about 88 weight percent of its particles are smaller than 3/8 of an inch. In the fourth step of this process, the fine and coarse carbonaceous fractions are mixed until a grinding mixture with the desired composition is obtained. The grinding step of the process of this invention . , . , In the process of this invention, the aforementioned grinding mixture * is wet ground until a slurry with specified properties is obtained. Thus, jn general, the grinding is continued to produce a stable, solids-liquid slurry comprising a consist of finely-divided particles of solid carbonaceous material dispersed in said liquid, wherein: (a)said slurry is comprised of at least 60 volume percent of said solid carbonaceous material(dry basis) , less than 40 " volume percent of said liquid, and, optionally,, from 0.01 to 4.0 weight percent (by weight of dry solid carbonaceous material) of dispersing agent; (b)said slurry has a yield stress of from 3 to 18 Pascals and a Brookfield viscosity at a solids content of 70 volume percent, ambient temperature, ambient pressure, and a shear rate of 100 revolutions per minute of less than 5,000 centipoise; (c)said consist has a specific surface area of from 0.8 to 4.0 square meters per cubic centimeter and an interstitial porosity of less than 20 volume percent; (d)from 5 to 70 volume percent of said particles of solid carbonaceous material are of colloidal size, being smaller than about 3 microns; (e)said consist of finely-divided particles of solid carbonaceous material has a particle size distribution substantial ly in accordance with the following formula: vhere I -Λ - 1.0 and vhere 1£ D < D - 0.0 end where if D > D 1.0 wherein: 1. CPFT is the cumulative percent of said solid carbonaceous material finer than a certain specified particle size D, in volume percent; 2. k is the number of component distributions in the consist and is at least I; 3. X. is the fractional amount of the component j in the consist, is less than or equal to 1.0, and the sum of all of the X. 's in the consist is 1.0; 4. n is the distribution modulus of fraction j and is greater than about 0.001; 5. D is the diameter of any particle in the consist and ranges from about 0.05 to about 1180 microns; 6. D is the diameter of the particle in fraction j , measured at 1% CPFT on a plot of CPFT versus size D , is less than D. , and is greater than 0.05 microns; 7. Di is the diameter of the size modulus in fraction j , measured by sieve size or its equivalent, and is from about 10 to about 1180 microns; and (f)the net zeta potential of said colloidal size particles 5 of solid carbonaceous material is from 15 to 85 millivolts. The slurry produced by the grinding process of this invention preferably has a yield stress of 5 to 15 Pascals and, more preferably, of 7 to 12 Pascals. The yield stress is the stress which must be exceeded before flow lOstarts. A shear stress versus shear rate diagram for a yield pseudoplastic or a Bingham plastic fluid usually shows a non-linear hump in the rheogram at the onset of flow; extrapolating the relatively linear portion of the curve back to the intercept of the shear stress axis gives the yield stress. 15 The Brookfield viscosity of the slurry produced by the process of this invention is preferably less than 4,000 centipoise. The Brookfield viscosity is tested after the solids concentration of the slurry is adjusted to 70 volume percent(the slurry is eithe diluted or concentrated until it has this concentration of solids) at ambient temperature, ambient pressure, and a 20shear rate of 100 revolutions per minute. It is more preferred that the viscosity of the slurry be less than 3,000 centipoise. In an even more preferred embodiment, the viscoisty of the slurry is less than 2,000 centipoise. In the most preferred embodiment, the viscosity of the slurry is less than 1,000 centipoise. 25 The term "Brookfield viscosity", as used in this specification, describes viscosity as measured by conventional techniques by means of a Brookfield Synchro-Lectric Viscosimeter(manufactured by the Brookfield Engineering Laboratories, Stoughton, Mass., U.S.A.). The solids-liquid slurry produced by the process of this invention 30 contains a consist of finely-divided particles of solid carbonaceous material dispersed in the liquid. Said consist preferably has a specific surface area of from 0.8 to 3.0 square meters per cubic centimeter. It is more preferred that the specific surface area be from 0.8 to 2.4 square meters per cubic centimeter,and it is even more preferred that the specific surface area be from 0.8 to 2.0 square meters per cubic centimeter. As used in this specification, the term "specific surface area" refers to the summation of the surface area of equivalent spheres in the particle size distribution as measured by sieve analysis and sedimentation techniques; the particle size distribution of the consist in the slurry is first determined, it is assumed that all of the particles in the consist are spherical , and then one calculates the surface area based on this assumption. As used herein, the term "consist" refers to the particle size distribution of the solid phase of the solids-liquid slurry. For any given consist , one can determine the particle size distribution by means well known to those skil led in the art. For measuring particle sizes and for determining particle size distributions of pulverized and fine grind carbonaceous particles used for preparing a carbonaceous slurry, the fol lowing two methods can be used and are preferred: 1. U.S. Series sieves Nos. 16, 20, 30, 40, 50, 70, 100, 140, 200, and 270 are used to determine weights of carbonaceous particles passing through each sieve in the range of (-) 1180 microns to (-) 53 microns. The cumulative volume percents of particles, dry basis, finer than(CPFT) a particular stated sieve size in microns is charted against the sizes in- microns on a log-log chart, referred to herein as a "CPFT chart" , to indicate the nature of the particle size distribution of 16 mesh x 270 mesh particles. 2. A Sedigraph 5500L(made by Micromeritics Co., Nbrcross, Ga., U.S.A.) is used to measure particle sizes and numbers of particles in the carbonaceous material and in the slurry in the range of (-) 75 microns to about 0.2 mm. The Sedigraph 5500L uses photo-extincition of settling particles dispersed in water according to Stoke 's law as a means of making the above determinations. Other instruments, such as a Coulter Counter or combinations of the Leeds & Northrup Microtrac Particle Analyzers can also be used for similar accuracy. The results can be plotted on a CPFT chart. Although these data do not necessarily extend to the size axis at 1% CPFT, the "Dj- at l%" can be determined by extrapolating the CPFT chart line to this axis and reading the intercept. This number, although not the true Dr , can be effectively used in a computer algorithm to determine % porosity and specific surface area. In addition to the above methods, particle size measurements can be estimated from methylene blue index measurements to obtain an approximate QMPI - ^i ATlO determination of the weight percent of colloidal particles of size below I mm. Such a procedure is described in A.S.T.M. Standard C837-76. This index can be compared with the surface area calculated by the CPFT algorithm. Once the particle size distribution of the consist is determined, it is assumed that each particle in the consist is spherical with a surface area of JT£)*;the diameter of D of the particles in each class of particles in the consist is known; and the surface area of the particles in each class is calculated and summed. The consist in the slurry produced by the process of this invention has an interstitial porosity of less than about 20 volume percent. It is preferred that said interstitial porosity be less than about 15 volume percent, and it is even more preferred that said interstitial porosity be less than about 10 volume percent. The interstitial porosity is a function of the volume of the interstices between the particles in the slurry consist. For any given space full of particles, the interstitial porosity is equal to the "minimum theoretical porosity" in accordance with the equation presented * below. Minimum Theoretical Porosity = 40% ( I - [l/VA] ) where VA is as defined by the following modified Westman-Hugiil algorithm: VA 2 = * A 2 X 2 i-1 Ai = , SX j ÷ AiXi 10 15 wherein: A^ a Apparent volume of a monodispersion of the ith 3 i Zβ particle, .. . , Xi = Mass fraction of the i tn size particles, VAi " Apparent volume calculated with reference to the i th size particles, 20 n = Number of particle sizes , and VA s Maximun value of VAj ^ s Apparent volune of the mixture of n particle sizes . To determine the interstitial porosity of any consist , the particle size distribution of said consist can be determined by the method described above " with reference to the measurement of the specific surface area. Thereafter, it is assumed that each particle in the consist is spherical , the volume of the particles is calculated in accordance with this assumption, and the interstitial porosity of the consist is then calculated in accordance with the above formula. It is noted that this calculated porosity is less than • 3 Λ . the true porosity of the consist as meaured, for example, by liquid loss due to the non-spherical morphology(shape) of the particles, and by invocation of D at 1%. s The slurry produced by the process of this invention contains a consist 5 which preferably is comprised of from 5 to 70 weight percent of colloidal particles. As used herein, the term "colloidal" refers to a substance of which at least one component is subdivided physically in such a way that one or more of its dimensions lies in the range of 100 angstroms and 3 microns. As is known, these are not fixed limits and, occasionally, systems containing larger particles are classifed as colloids. It is preferred that, in the carbonaceous consist of the slurry of this invention, at least 5 weight percent of the carbonaceous particles are smaller than 3.0 microns and, more preferably, that from 5 to 70 weight percent of said particles are smaller than 3.0 microns. In one of the preferred embodiments, from 5-30 weight percent of the carbonaceous particles are smaller than 3.0 microns. In another of the preferred embodiments, from 7-20 weight percent of the carbonaceous particles are smaller than 3.0 microns. The slurry produced by the process of this invention comprises a compact of finely-divided carbonaceous particles dispersed in fluid such as, e.g., finely-divided coal particles dispersed in water. The term "compact", as used in this specification, refers to a mass of finely- divided particles w t hich are closely packed in accordance with this invention. In the aforementioned CPFT formula: (l)k is preferably from I to 30, and most preferably is I; (2)n is the distribution modulus(or slope) of fraction j , is preferably from 0.001 to 10, more preferably from 0.01 to 1.0, and most preferably from 0.01 to 0.5; (3)D is the diameter of the smallest particle in fraction j(as measured by extrapolating the CPFT chart line, if necessary, to one percent CPFT using data from sieve analyses plus the Micromeritics Sedigraph 5500L); 4)D^ preferably is from 30 to 420 microns and most preferably is from 100 to 300 microns. D|_ is the theoretical size modulus of the particle size distribution; when CPFT is plotted against size, the Dj_ value is indicated as the intercept on the upper X axis of the CPFT/D plot. However, as is known to those skilled in the art, because of aberrations in grinding the coars end of a particle size distribution, the actual top particle size is always larger than the D|_ obtained by, e.g., the particle size equation described in this case; thus, e.g., a D^ size modulus of 250 microns will usually produce a particle distribution with at least about 98 percent of the particles smaller than 300 microns. Consequently, slurry produced by the "BXJRl^; , . - -- OQMMPPII ^ . process of this invention has a compact which is substantially in accordance with the CPFT equation; minor deviations caused by the actual top size being greater than the D _ are within the scope and spirit of the invention. In one of the preferred embodiments, the slurry produced by the process of this invention is a coal-water slurry with a net zeta potential of from 15 to 85 millivolts. The following discussion of zeta potential will refer to a coal-water slurry, it being understood that the discussion is equally applicable to other slurries such as, e.g., a coke-water slurry. As used in this specification, the term "zeta potential" refers to the net potential , be ' , it positive or negative in charge; thus, a zeta potential of from 15.4 to 70.2 millivolts includes zeta potentials of from -15.4 to -702 millivolts as well as zeta potentials of 15.4 to 70.2 millivolts. It is preferred that the zeta potential of said slurry be from 30 to 70 millivolts. As used in this specification, the term "zeta potential" has the meaning given to it in the field of colloid chemistry. Zeta potential can be measured by conventional techniques and apparatus of electroosmosis. In the present invention, a Pen Kem System 3000(made by Pen Kem Co. Inc. of Bedford Hills, N.Y.) was used for determining the zeta * otential in the examples herein. This instrument is capable of automatically taking samples of coal particles and producing an EPM distribution by Fast Fourier Transform Analysis from which the average zeta potential can be calculated in millivolts. The zeta potential is measured using very dilute samples of the < 10 micron sized coal particles in the coal compact. It is preferred that the zeta potential of the colloidal sized coal particles in the coal consist of the slurry be negative in charge and be from -15.4 to -70.2 millivolts. It is more preferred that said zeta potential be from -30 to -70 millivolts. One preferred means for measuring the zeta potential is to grind a sample of coal in either a laboratory size porcelain ball mill with porcelain balls in distilled water at 30 weight percent for approximately 24 hours or in a steel ball mill with steel balls at 30 weight percent solids for 16 hours, or until all of the particles in the coal are less than 10 microns in size. Small samples of this larger sample can then be 4 ΓATIO prepared in a known way by placing them in a vessel equipped with a stirrer with a sample of water to be used as a carrier in the coal- water slurry. Various acidic and basic salts are then added in incremental amounts to vary the pH , and various cncentrations of various candidate dispersing agents are likewise added in incremental amounts. These samples are then evaluated in any electrophoretic mobility, electroosmosis, or streaming potentail apparatus to determine electrical data,from which the zeta potential is calculated in a known way. Plots " of zeta potential , pH , and specific conductance vs. concentration may then be made to indicate candidate surfactants, or combinations thereof, to be used to produce the optimum dispersion of coal particles in the carrier water below the amount at which dilatancy may be reached. Illustration of the grinding process Several typical means of practicing the invention are i llustrated in Figure 2. In a wet grinding method, carbonaceous material is charged to crusher 10 and crusher 12. In one embodiment, it is preferred that one carbonaceous material be charged to crusher 10 and another carbonaceous material be charged to crusher 12. In another preferred embodient , different types of the same carbonaceous material are charged to crushers 10 and 12. In the latter preferred embodient, the carbonaceous material charged to crushers 10 and 12 can be coal ; thus, e.g., a coal fr-action which contains less than 30 weight percent of volatilizabie hydrocarbons(such as anthracite or lo volatile bituminous coal) can be charged to crusher 10, and a coal fraction which contains more than about 35 weight percent of volatilizabie hydrocarbons(such as lignite or high volatile bituminous coal) can be charged to crusher 12. - Any of the crushers know tothose skilled in the art to be useful for crushing carbonaceous material can bve used as crusher 10 and/or crusher 12. The same crusher can be used for crushers 10 or 12, or different crushers can be used. Thus, one can use a rod mil l , a gyratory crusher, a roll crusher, a cage mill , and the like. Generally the carbonaceous material is crushed to a size of about 1/4" x 0, although coarser and finer fractions can be used. The crushed material from crusher 10 is fed through line 14. The O PI crushed material from crusher 12 is fed through line 16. Part or all of the crushed material from crusher 10 can be mixed with part or all of the crushed material from crusher 12 by passing the crushed material in line 14 and/or the crushed material in line 16 through transfer line 18. Alternatively, transfer line 18 can be closed, the crushed material from crusher 10 can be fed directly to mil l 26, and the crushed material from crusher 12 can be fed directly to dry grinder 24. The crushed material from either crusher 10 or 12 can be sampled and measured for pH in the pH meter 13, which wi ll be discussed later, thus establishing a baseline for the control circuit discussed later. The crushed material from crusher 10 can be fed through line 14 to mill 26. Mill 26 can either be a tumbling miil(such as a ball mill , pebble mi ll , rod mill , tube mill , or compartment mi ll); a non-rotary ball or bead mil l, such a stirred ball mills( including the Swecon dispersion mi ll , the Attritor, etc.) ; a vibratory mil l ; and the like. In one preferred embodiment , mill 26 is a ball mil l which, preferably, is run at a reduced speed. In this embodiment, the mixture is ground at a high solids content of from 60 to 82 volume percent of carbonaceous material and at a ball mil l speed of from 50 to 70 percent of the ball mill critical speed. The critical speed of the bal l mill is the theoretical speed at which the centrifugal force on a bal l in contact with the mi ll shell at the height of its path equals the force on it due to gravity, and it is defined by the equation: wherein Nς is the critical speed(in revolutions per minute), and D is the diameter of the mil l(in feet) for a ball diameter that is small with respect to the mil l diameter. It is preferred to run ball mill 26 at less than 60 percent of its critical speed and, more preferably, at less than 55 percent of its critical speed. The use of reduced critical speed grinding produces a slurry with improved viscosity and stability properties. In general, mill 26 will have sufficient carbonaceous material and liquid fed to it so that it will contain from 60 to 82 volume percent of carbonaceous material. Crushed material is fed to mill 26 thorugh line 14. Alternatively, or additionally, milled carbonaceous material(which might or might not contain carrier liquid, such as water) from mil l 26 can be recycled through line 40 back into mil l 26; this recycled milled carbonaceous material can either be fine milled material which passes through a sieve bend 38 and/or coarser mi lled material which does not pass through sieve bend 38, Alternatively, or additionally, milled carbonaceous • c material from mill 46(which preferably contains carrier liquid) can be recycled into mill 26 through lines 48, 58, or 60, or into mi ll 46 through line 61. Alternatively, or additionally, carbonaceous material(which preferably contains carrier liquid) which has been mixed in high shear mixer 64 can be recycled back into mill 26 through lines 66 and 60, or into mill ig 46 through line 61. Carrier liquid is fed to mill 26 through line 20. A sufficient amount of said carrier liquid is fed into the mill 26 so that, in combination with all of the other feeds to mill 26, a solid-liquid mixture which contains from 60 to 82 volume percent of carbonaceous material is produced. In general, 15 one charges from 0 to 10 volume percent more solid carbonaceous material to mill 26 than is desired in the final slurry product, provided that in no event is more than 82 volume percent of such material charged to the mill. Dispersing agent may optionally be added to the mill 26 through line 22. In general , a sufficient amount of dispersant is added through line 22 0 and/or line 62 and/or line 88 so that the slurry in mill 26 contains from 0.01 to 4.0 weight percent of one or more dispersing agents, based on the weight of dry carbonaceous material. A portion of the milled slurry from mill 26 is passed via line 28 through " viscometer 30, density meter 32, pH meter 33, and line 27 back to 5 line 28; a portion of the slurry passed to density meter 32 is also passed to particle size distribution analyzer 34. The function of viscometer 30, density meter 32, pH meter 33, and particle size distribution analyzer 34 is to continually monitor the quality of the slurry being produced in mill 26 so that, if necessary, the process can be adjusted by adjusting the 0 feeds of solids and/or solids/fluid slurry and/or liquid and/or dispersant and/or ground carbonaceous materialto the mill. Any of the viscometers known to those skilled in the art can be used as viscometer 30. Thus, one can use a Nametre Viscometer. The viscometer 30 indicates the viscosity of the ground slurry. If the viscosity of the ground slurry is higher than desired, the underflow slurry is subjected to further tests(in density meter 32, pH meter 33, and particle size distribution analyzer 34). Any of the density meters known to those skilled in the art can be used as density meter 32. Density meter 32 indicates the density of the slurry, which directly varies with the solids content. If the density of the slurry is lower or higher than desired, the slurry is subjected to further tests in particle size analyzer 34 to determine the particle size distribution of the underflow slurry and its attendant surface area and porosity. Any of the pH meters known to those skilled in the art can be used as pH meter 33. The pH meter measures the hydrogen ion concentration of the slurry. Particle size distribution analyzer 34 analyzes the particle size distribution of the compact of the underflow slurry. Any of the particle size distribution analyzers known to those skilled in the art such as, e.g., Micromeritics Sedigraph 5500L, Coulter Counter, Leeds and Northrup Microtrac Particle Analyzers, can be used as analyzer 34. From the data generated by analzyer 34, the specific surface area and the porosity of the compact of the underflow surry can be determined. Ground slurry from mill 26 is passed through line 28 to sieve bend 38. Sieve bend 38 may be 40 mesh sieve which, preferably, allows underflow slurr of sufficient fineness(such as, e.g., less than 420 microns) through to line 29 into mill 46, where it is subjected to further grinding; alternatively, all or part of this fine ground slurry can be recycled into mill 26 via line 40. Overflow particles which are greater than 420 microns are recycled via line 40 into mill 26, where they are subjected to further grinding. The ground slurry from mill 26 which passes through sieve bend 38 can be passed through line 29 to mill 46. Mill 46 can be a rod mill , a ball mill , or a stirred ball mill. It is preferred that the slurry be ground in mill 46 until at least 95 volume percent of the particles in the slurry have diameters less than 20 microns, preferably less than 15 microns, and more preferably less than 5 microns. A portion of the ground slurry from mill 46 is passed through a control circuit comprised of viscometer 50, density meter 52, particle size distribution analyzer 54, pH meter 53, and line 56, wherein the slurry is analyzed as described above for the slurry passing from line 28. The feed to mill 46 can be adjusted by feeding crushed carbonaceous material from a dry grinding mill 24 and/or adjusting the feeds to mill 26. Slurry from density meter 52 is returned through line 56 to line 48. Part or all of ground slurry from mill 46 can be passed through lines 48, 58, and 60 back to mill 26, wherein it is fed as a recycle stream. Alternatively, or additionally, part or all of ground slurry from mill 46 can be passed via line 61 to mill 46 as a recycle stream. Alternatively, or additionally, part or all of ground slurry from mill 46 can be passed into high sehar mixer 64. Any of the high shear, high intensity mixers known to those skilled in the art can be used as high shear mixer. Thus, one can use a Banbury mixer, a Prodex-Henschel mixer, a Weiex-Papenmeir mixer, and the like. Dispersing agent is preferably passed through line 62 to high shear mixer 64 to optimize the zeta potential of the colloidal particles in the mixer. A sufficient amount of dispersant is preferably charged to this mixer so that the final coal slurry product contains from 0.01-4.0 weight percent of dispersant, by weight of dry coal. Some or all of the product from high shear mtxer 64 can be recycled via lines 66 and 60 to ball mill 46. Alternatively, or additionally, some or all of the product from high shear mixer 64 can be fed through line 68 to hopper 70 and thence to Moyno pump 74 for volumetric blending. The "Moyno pump" , also referred to as a "progressive cavity" or "moving cavity" pump, is well known to those skilled in the art. It consists of a convoluted hardened steel rotor and an inverse convoluted elastomeric stator so designed that, as the rotor turns, it maintains full contact with the stator one one side and only point to point contact with the stator on the other side. This produces a sealed cavity which moves in the direction of discharge as the rotor turns. Using a variable speed drive this pump can deliver variable flow volumes at reasonable pressures and at high viscosities. Using a pair of pumps as 74 and 75 allows accurate blending volumetrically of two converging streams of fluids. The function of the Moyno pump in the process is to deliver the proper volumetric proportions of two streams from lines 68 and 42 or hoppers 70 and 72 to line 73 to low shear blender 76 via line 73. The blend from blender 76 is then transferred via line 77 using Moyno pump 78 through line 80 to a cleaning apparatus 82. Material from Moyno pump 74 can be fed through line 73 to low shear blender 76. Any of the low shear blenders known to those skilled in the art can be used. Thus, by way of illustration and not limita- tion, one can use a twin-blade conical mixer (Atlantic Research Corp.), a double-arm kneader mixer (Baker Perkins Inc.) , a helical ribbon mixer, gate mixers, Poly-Eon continuous reactors (Baker Perkins), the Rietz Extructor, Ko- neader (Baker Perkins), Transfer mix (Sterling Extruder Corp.), Rotofeed (Baker Perkins), ZSK (Wemer-Pfleiderer), Halo-flite Processor (Joy Mfg. Co.), Kneadermaster (Patterson Industries Inc.), etc. Thereafter, the product from low shear blender 76 can be fed through line 77 to Moyno pump 78 and thence through line 80 to cleaner 82. Cleaned slurry from cleaner 82 can be passed through line 83 to high shear mixer 86. Alternatively, or additionally, cleaner 82 can be bypassed in whole or in part and product from Moyno pump 78 and/or mill 24 can be passed through lines 17 and 84 to high shear mixer 86. Required amounts of dispersant and liquid are fed in lines 88 and 90, respectively to the high shear mixer. A final control circuit, comprised of viscometer 94, density meter 96, line 92, particle size distribution analyzer 98, zeta meter 100, ash and sulfur analyzer 102 and ph meter 103, allows one to analyze a portion of the slurry being produced In high shear mixer 86 so that appropriate adjustments can be made in the feeds. Any of the zeta meters known to those skilled in the art can be used as zeta meter 100. Similarly, any of the ash and sulfur analyzers known to those skilled in the art can be used as analyzer 102. Figure 2 also illustrates a dry grinding process for making the slurry of this invention. In this process, which may be used separately and/or in conjunction with the wet grinding process, crushed solid carbonaceous material from crusher 12 is passed through line 16 to dry grinder 24; part or all of the material from crusher 12 may alternatively be passed through transfer line 18 to be mixed with solid carbonaceous material from crusher 10 and thence passed through line 14 to mill 26. Any of the dry grinders known to those skilled in the art can be used as grinder 24. Thus, by way of illustration and not limitation, one can use a hammer mill. Thus, e.g., one can also use ball mills or the ring roller mills described on pages 8-33 and 8-34 of Perry and Chilton's Chemical Engineer's Handbook, 5th edition, supra. It is preferred to ground the crushed material in dry grinder 24 until it is pulverized, that is until it is a consist of about 40 mesh by 0. The pulverized solid carbonaceous material from dry grinder 24 can be passed through line 44 to mill 46 wherein it may be mixed with the feed from line 29 (or, alternatively, not mixed with any such additional feed) and thereafter processed as described hereinabove. Alternatively, or additionally, part or all of the pulverized material from dry grinder 24 can be passed through line 15 and line 14 to mill 26. Alternatively or additionally, part or all of the pulverized carbonaceous material from dry grinder 24 can be passed though line 17 and fed directly into high shear mixer 86, where it is blended with liquid and dispersant and ground to-make carbønaceous material-liquid slurry. In another embodiment, illustrated in Figure 2, part of all of the underflow slurry which passes through sieve 38 can be passed through line 42 to hopper 72 and thence to Moyno pump 75. The product from Moyno pump 75 is then passed through line 73 to low shear blender 76 and processed as described above. The operation of the control cirucit comprised of viscometer 94, density meter 96, particle size distribution analyzer 98, zeta meter 100, and ash and sulfur analyzer 102 will now be described, it being understood that the other control circuits in the process operate in a similar manner. In Fig. 2, control circuits are shown which are comprised of a viscometer, a densitometer, a particle size analyzer, and a pH meter. As will be apparent to those skilled in the art, fewer or more such control circuits can be used in the process, and the control circuits can be located at points in the process other than those indicated in Fig. 2. A typical control circuit is comprised of viscometer 30, densito- meter 32, particle size analyzer 34, and pH meter 33. This circuit continually monitors the viscosity, density, consist particle size distribution, and pH of the slurry, and it adjusts the process so that these factors are properly interrelated. If the density of the slurry is not within the target range, or if the viscosity is too low, then the control circuit determines this and adjusts the ratio of the solids flow rate in the process to the liquids flow rate in the process, thereby adjusting the solids/liquids ratio. If the viscosity of the slurry is higher than the target range, then the control circuit determines this and adjusts the dispersant concentration (insufficient dispersant can cause a viscosity increase), the solid and/or the liquid flow rate (an insufficient liquid flow rate will cause the solids/liquids ratio to be too high, and will thus cause the viscosity to increase), the pH (if the pH of the grinding mixture is too low, the viscosity might be too high), and/or the particle size distribution. The pH of the grinding mixture can be adj'usted by adding more dispersant and/or caustic. It is to be understood that all of these factors are interrelated, arid that the control circuit can, and preferably does, monitor and adjust all of these factors simultaneously. For any given solids-slurry system, the target particle size distribution can be determined by analyzing "ideal" slurry and determining its particle size distribution; an "ideal" slurry is one which has the required solids content and viscosity and which fits into the equations described elsewhere in this specification. The particle size distribution of this "ideal slurry" can be determined on two Leeds and Northrup Microtrac Particle Analyzers-the Extended Range Analyzer (300 - 3 ym) and the Small Particle Analyzer (21 - 0.1 μm). The percent of the particles in the slurry consist which are less than 300 microns, 212 microns, 150 microns, 106 microns, 75 microns, 53 microns, 38 microns, 27 microns, etc. can be determined. Then, armed with this particle size profile for the ideal slurry, the particle size analyzer in the control circuit can continually analyze the particle size distribution of the slurry in the process and, if it is less than ideal, the control circuit can adjust the process accordingly. "guTCt ( _ OMPI IPO v - ?ttATlO In general, the percent of the particles in the slurry consist which are less than a certain specified particle size can be adjusted by adjusting the relative feed rates of the solids and the liquids fed to the system. For example, if the particle size analyzer indicates that 5 the percent of the particles in the consist less than 212 microns is not within the target range, this can be adjusted by varying the dry carbonaceous material feed rate. For another example, a change in the entire particle size distribution of the slurry consist, including the percent less than 212 ym, can be made by varying the solids/liquids ratio, r i.e., by adjusting the volume percent solids in the grinding mixture. Of particular importance in the particle size distribution, analysis is * the contorl of the "n" and the specific sur ace area of the slurry consist. The "n" in the particle size distribution equation is proportional to the difference between the weight percent concentrations 15 of two selected channels in the Microtrac ER analyzer; the difference between the weight percent concentrations of, e.g., particles less than L50 microns'and partifcles less than 53 microns can be determined for the aforementioned "ideal" alurry; and, armed with this "ideal difference" between said concentrations, the particle size analyzer can continually 20 determine this difference for the slurry in the process and, if it varies from the ideal, the control circuit can adjust the relative feed rates of the solids and liquids fed to the system. The specific surface area of the consist in the slurry is proportional to the difference between the weight percent concentrations of two selected 5 channels in the Microtrac SPA analyzer; the difference between the weight percent of e.g., particles less than 1.01 and 0.34 microns can be determined for the aforementioned "ideal slurry"; and, armed with this "ideal difference", the particle size analyzer can continually determine this difference for the slurry in the process and, if it - 30 varies from the ideal, the control circuit can adjust the relative feed rates of the solids and liquids fed to the system. The control system described in Fig. 2 is capable, thus, of continually monitoring and adjusting the slurry solids content, the slurry viscosity, the particle size distribution of the slurry consist, the "n" of the slurry consist, and the specific surface area of the slurry is higher than the target rate, the control circuit determines this and can adjust the dispersant concentration and/or the solid flow rate and/or the liquid flor rate and/or the pH. Alternatively, or additionally, the control circuit can adjust the amount of reground carbonaceous fine material being recycled to the grinding mill; an insufficient amount of colloidally sized carbonaceous material in the slurry consist will cause the viscosity of the slurry to be too high, and the addiiton of finely ground carbonaceous material to such a slurry tends to reduce its viscosity. For example, if viscometer 30 determines that the slurry in mill 26 is too viscous, it can cause finely ground carbonaceous material from mill 46 and/or high shear mixer 64 to be recycled through line 60 to mill 26, thereby increasing the amount of fine material in the grinding mixture in mill 26 and tending to lower its viscosity. For example, if viscometer 94 determines that the slurry in high shear mixer 86 is too viscous, it can cause finely ground carbonaceous material from mill 46 and/or high shear mixer 64 to be recycled through line 60 to mill 26, thereby increasing the amount of fine material in the slurry ultimately fed to high shear mixer 86 through line 84; it can recycle finely ground carbonaceous material from mill 46 through lines 48, 58, 60, and 61 back into mill 46; it can recycle finely ground carbonaceous material from high shear mixer 64 through lines 66, 58 and 48 back into high shear mixer 64; it can recycle finely ground carbonaceous material from mill 26 through lines 28 and 40 back into mill 26; it can do any combination of the aforementioned means of increasing steps; and the like. The afore¬ mentioned means of increasing the amount of finely ground carbonaceous material in mills 26 and 46 and mixers 64 and 86 are only illustrative, and those skilled in the art upon an examination of Fig. 2 will appreciate other means which can be used. Thus, the control circuit can adjust the viscosity of the slurry in mill 26 by adjusting the amount of carbonaceous material fed through line 14, the amount of carbonaceous material fed through lines 16 and 18, the amount of carbonaceous material fed through line 15, the amount of carrier liquid fed through line 20, the amount of dispersant fed through line 22, the amount of finely ground carbonaceous material recycled through lines 28 and 40, the amount of finely ground carbonaceous material recycled through lines 48, 58, and 60, the amount of finely ground carbonaceous material recycled through lines 66 and 60, and/or the pH. Thus, the control circuit can adjust the viscosity of the slurry in mill through lines 66 and 60, and/or the pH. Thus, the control 46,by adjusting any or all of the aforementioned factors, can influence the slurry viscosity in mill 26, (for the properties of the slurry coming out of mill 26 influence the properties of the slurry formed in mill 46), and, additionally or alternatively, the amount of carbonaceous material fed to.mill 46 through line 44, and the amount of carbonaceous material fed to mill 46 through line 29. Thus, the control circuit can adjust the viscosity of the slurry in high shear mixer 64 by adjusting any or all of the aforementioned factors influencing the slurry viscosity in mills 26 and 46 (for when the properties of these slurries are changed, they change the properties of the slurry in mixer 64) and, alternatively or additionally, the amount of dispersing agent added through line 62, and the amount of finely ground carbon¬ aceous material recycled through lines 66 and 58 to mixer 64. Thus, the control circuit can adjust the viscosity of the slurry in high shear mixer 86 by adjusting any of the aforementioned factors influencing the slurry viscosity in mill 26, mill 46, and high shear mixer 64, and, alternatively or additionally, the amount of dispersing agent fed to mi-^er 86 through line 88, the amount of carrier liquid fed to mixer 86 through line 90, the amount of dry carbonaceous material fed to high shear mixer through line 17, the amount of finely ground carbonaceous material fed through line 42 to hopper 72, the pH of the slurry in mixer 86, and the like. Cleaer 82, referred to in Fig. 2, can be any of the carbonaceous slurry cleaning apparatuses known to those skilled in the art. Thus, by way of illustration and not limitation, one can use the electro¬ phoretic deashing cell illustrated on page 3 (Fig. 3) of Miller and Baker's Bureau of Mines Report of Investigations 7960 (United States Department of the Interior, Bureau of Mines, 1974). the disclosure of which is hereby incorporated by reference into this specification. Thus, one can clean said slurry by passing it onto a sedimentation device, such as a lamella filter, where it is allowed to settle. Thus, one can effect magnetic separation of the slurry and/or combine such magnetic separation with sedimentation in the form of a pre- or post- treatment step. In one preferred embodiment, cleaner 82 involves the cleaning process described in U.S. patents 4,186,887, and 4,173,530, the disclosures of which patents are hereby incorporated by reference into this application. In this preferred embodiment, it is preferred that no dispersing agent be added to the coal-fluid mixture until after the mixture has passed through cleaner 82 into high shear mixer 86, at which time the required amount of dispersant is added; thus, in this preferred embodiment, no dispersing agent is added to mill 26. In one preferred embodiment, the carbonaceous solid material in the grinding mixture (and in the slurry produced therefrom) contains less than about 5 weight percent of ash. The term "ash", as used in this specification, includes non-a-carbonaceous impurities such as, e.g., .•inorganic sulfur, various metal sulfides, and other metal impurities.. as well as soil and clay particles, The fraction of ash in the carbonaceous material can be calculated by dividing the weight of all of the non-carbonaceous material in the slurry solids by the total weight of the slurry solids (which includes both carbonaceous and non-carbonaceous material). It is preferred that the slurry produced by the process of this invention have a pH from, about 5 to about 12 and, preferably, from abβut 7 to about 11. Conventional means may be used to adjust the pH of the slurry so that it is within these ranges. In one preferred embodiment, the slurry produced by the process of this invention possesses a unique property; its viscosity decreases at a constant shear rate with time, at an increasing shear rate, and at an increasing temperature; this property greatly enhances the pumpability of the slurry. In one embodiment, the slurry produced by the process of this invention is a yield-pseudoplastic fluid. The term "yield pseudoplastic fluid", as used in this specification, has the usual meaning associated with it in the field of fluid flow. Specifically, a yield pseudoplastic fluid is one which requires that a yield stress be exceeded before flow commences, and one whose apparent viscosity decreases with increasing rate of shear. In a shear stress vs. shear rate diagram, the curve for a yield pseudoplastic fluid shows a non-linearly increasing shear stress with a linearly increasing rate of shear. In a "pure" pseudoplastic system, no yield stress is observed so that the curve passes through the origin. However, most real systems do exhibit a yield stress, indicating some plasticity. For a yield pseudoplastic fluid, the viscosity decreases with increased shear rate. The following examples are presented to illustrate the claimed invention but are not to be deemed limitative thereof. Unless other¬ wise stated, all parts are by weight and all temperatures are in degree centigrade. Example 1 - Preparation of coal/water slurry Three hundred thirty-five pounds of 4 x 0 Ohio No..6 bituminous coal with a Hardgrove Grindability Index (HGI) of 50 and a free swelling indes (FSI) of 3.5, .6.0 poinds of water, 0.1 weight % (0.1 weight %) of sodium hydroxide, and 1.1 wgt. %, (1673 grams) of Lomar D (the sodium salt of a condensed alkyl monomaphthalene sulfonic acid sold by the Diamond Shamrock Process Chemicals, Inc. of Morristown, New Jersey) were charged in a Kennedy Van Saun 3 foot diameter x 5 foot long ball mill (manufactured by the Kennedy Van Saun Co. of Danville, Pennsylvania). The ball mill had 35 volume % of a 2.0 inch top Bond ball charge and was comprised of 34 weight % of balls of 2.0 inch diameter, 43 weight % of balls of 1.5 inch βiameter, 17 weight % of balls of 1.25 inch diameter, and 6 weight % of balls of 1.0 inch diameter. The ball mill was run at a speed of 33 revolutions per minute, which corresponded to 70 percent of the critical speed of the ball mill. Grinding was conducted in the mill under these conditions until about 98.5 weight percent of the coal particles passed through a 50 mesh screen; during the grinding, samples of the slurry were periodically evaluated to determine the fineness of the coal in the slurry. The particle size distribution of the slurry produced in the ball mill was determined by sieve analysis and by Sedigraph 5500L analysis. The sieve analysis Indicated the amount of coal particles In the slurry consist which ranged from about 53 microns (270 mesh) to the largest size coal particle in the slurry (about 1180 microns). The Sedigraph analysis indicated the amount of coal particles in the slurry consist 5 which ranged from about 74 microns to the smallest size coal particle in the slurry which was present in a concentration of at least 1 weight percent. The sieve analysis data and the Sedigraph analysis data were then merged to yield the volume percent of the various sized particles in the slurry. Thereafter, based upon the assumption that 10 all of the particles in the slurry were spherical, the specific surface area and the porosity of the coal particles in the slurry consist were calculated. The slurry consist of this Example had a porosity of 8.096 volume 2 3 percent and a specific surface area of 1.015 m /cc . This slurry 15 produced a yield stress of about 1.0 - 2.0 Pascals at 70 volume percent solids and solids and unstable. The slurry had a Haake viscosity of 2500 cps at 100 sec , . Portions of unstable slurry produced in substantial accordance with this Example were diluted to concentrations of either 40 weight 20 percent, 50 weight percent, or 60 weight percent, and each of these diluted portions was separately ground in a Draiswerke stirred ball mill (model number PM 25-40 STS/DDA, manufactured by Draiswerke Inc. of Allendale, New Jersey). The 40 percent samples were fed to the ball mill at a feed rate of 100 pounds per hour; the 50 percent samples were *■ * ■ "' fed at a rate of 300 pounds per hour; the 60 percent samples were fed at a rate of 450 pounds per hour. The ball mill was run at an internal shaft speed of 520 r.p.m. The grinding media were 2 m.m. diameter steel balls. The product produced by the grinding at 40 solids in the Draiswerke stirred ball mill had a D of 64 ym and a median size of 30 21.6 ym; the surface area was 5.582 m2/cm3j and the porosity was 19.44 percent. The product produced by grinding at 50% solids in the Draiswerke stirred ball mill had a D. of 9.3 ym and a median size of 2.561 ym; the 2 3 surface area was 3.962 m /cm , and the porosity was 16.85 percent. The product by grinding at 60% solids in the Draiswerke stirred ball mill had a of 19.6 y and a median size of 4.766 μm; the surface area was 2.639 square meters per cubic centimeter, and the porosity was 12.69 volume percent. The procedure of Example 1 was repeated, with the exception that a different charge was put into an Abbe ball mill instead of a Kennedy Van Saun ball mill. The Abbe ball mill was model Double No. 2, manufactured by the Paul 0. Abbe Company of Little Falls, New Jersey; it had 35% volume of 2.0 inch top Bond ball size and was run at a speed of 34 revolutions per minute, which corresponded to 51 percent of the ball mill critical speed. Instead of using 100 weight percent of dry Ohio No. 6 bituminous coal, the charge now contained either 5 weight percent, 10 weight percent, or 15 weight percent of one of the reground coals produced in the Draiswerke stirred ball mill(by weight of coal) . The dry coal/slurry/water/ surfactant mixture was then ground in the Abbe ball mill in accordance with the procedure of this Example, but the surfactant concentration in the mixture was still 1.1 weight ρercent(no surfactant or caustic was added when the fine portions were ground) . The properties of the slurries obtained are indicated below in Table 1. Table 1 I weight * type Volume Porosity Surf". Bingham Zeta . ' slurry fines percent * area visσoa. pot. added to added solids m 2 /cm3 cP mV Abbe mill 0. 61 7. 3 o. ηb 1300 -13.36 5A "Of 61 6.90 1.16 1500 -12.67 10A 10* 61 10.97. 1.2 1250 -12.29 I5A •40* 61 6.21 1.80 1850 -11.59 5B 50* 61 7.17 1.08 1800 -38.5 '. 10B 50* 61 6.13 1.38 1150 -10.53 15B 50* 61 6.68 1.38 1700 -10.78 5C 60* 61 • 9.30 0.97 1350 -33.91 10C 60* 61 6.30 1.0.2 1850 -11.1J ' 15C 60* 61 1.99 1.18 1200 -11.521 Example 2 - Preparation of coail/water ιslurry A coal mixture comprised of a blend of coal from Virginia, Kentucky, and West Virginia was used; this coal was supplied by the United Coal Company of Bristol, Virginia, it had a Hardgrove grindability index of about 50, it had a volatile content(dry basis) of 42.25 percent, and it contained 1.66 weight percent of ash(on a dry basis) . A 7.23 pound portion of this coal together with 3.23 pounds of water were charged in an 8.0 inch diameter steel ball mill with 1/2 inch steel balls. Grinding was conducted at 50 percent ball charge loading at about 50 r.p.m. for about 20 hours. The ground coal produced in this ball mill was 99.5% less than 11.9 microns, with a median size of 8.23 microns. The surface area was 1.48 square meters per cubic centimeter. The porosity was 12.31 volume percent. A 13.85 pound sample of this coal was crushed in a roll crusher to a 4 x 0 mesh consist. The crushed coal was then charged to a 16.0 inch diameter Abbe mill with 2.0 inch top Bond ball charge together with the 4.60 pounds of the fine coal slurry produced in the 8.0 inch diameter mill, 3.28 pounds of water, 7.4 grams of caustic, and 51.8 grams of Lomar D surfactant. This mixture was ground until the mixture contained at least about 98.5 percent of coal particles which passed through a 50 mesh screen. The coal slurry thus produced contained no more than about 1.66 weight percent of ash(dry basis). The slurry had a viscosity at 71 weight percent solids and 100 sec. of 1030 centipoise. Particle size analysis of the coal consist of the slurry indicated that the consist had a porosity of 5.11 volume percent and a specific surface area of 0.94 square meters per cubic centimeter. It is to be understood that the foregoing description and Examples are illustrative only and that changes can be made in the ingredients and their proportions and in the sequence and combination of process steps as well as other aspects of the invention discussed without departing from the spirit and scope of the invention as defined in the following claims.

Claims: I claim: 1. A grinding mixture comprising from 60 to 82 volume percent of solid carbonaceous material, from 18 to 40 volume percent of carrier liquid, and from 0.01 to 4.0 weight percent, by weight of dry solid carbonaceous material, of dispersing agent, wherein: (a)said grinding mixture has a pH of from 5 to 12, (b)said grinding mixture contains at least two consists of solid carbonaceous material, (c)from 2 to 50 weight percent of said solid carbonaceous material is comprised of carbonaceous particles with a median particle size of from 0.05 to 40 microns, and (d)from 50 to 98 weight percent of said solid carbonaceous material is comprised of carbonaceous particles with a median particle size greater than 40 microns. 2-. The grinding mixture as recited in claim 1, wherein said solid carbonaceous material is a solid carbonaceous fuel. 3. The grinding mixture as recited in claim 2, wherein said solid carbonaceous material is coke. 4. xhe grinding mixture as recited in claim 2, wherein said solid carbonaceous material is coal. 5. The grinding mixture as recited in claim 4, wherein said liquid is a petroleum liquid selected from the group consisting of number 2 fuel oil, number 4 fuel oil, number 6 fuel oil, gasoline, naphtha, and mixtures thereof. # 6. The grinding mixture as recited in claim 4, wherein said liquid is a mixture of water and petroleum liquid. 7. The grinding mixture as recited in claim 6, wherein at least 90 weight percent of said carrier liquid is water and no more than 10 weight percent of said carrier liquid is petroleum liquid. 8. The grinding mixture as recited in claim 4, wherein said liquid is water. 9. The grinding mixture as recited in claim 8, wherein said grinding mixture is comprised of from 64 to 81 volume percent of coal. 10. The grinding mixture as recited in claim 9, wherein from OMPI 4 to 40 weight percent of the coal in the grindng mixture is comprised of coal particles with a median particle size of from 1 to 30 microns. 11. The grinding mixture as recited in claim 10, wherein from 60 to 596 weight percent of said coal in the mixture is comprised of coal particles with a median particle size greater than about 40 microns. 12. The grinding mixture as recited in claim 11, wherein the pH of said grinding mixture is from 7 to 11. 13. The grinding mixture as recited in claim 12, wherein from 6 to 1030 weight percent of the coal material in the mixture is comprised of coal particles with a median particle size of from 2 to 20 microns. 14. The grindng mixture as recited in claim 13, wherein from 70 to 94 weight percent of said coal in the mixture is comprised of coal particles with a median particle size greater than about 40 microns. 1515. The grindng mixture as recited in claim 14, wherein said mixture comprises from 75 to 80 volume percent of coal. 16. A process for preparing a solid-liquid slurry, comprising the steps of: (a)providing the grinding mixture of claim 1; and 0 (b)grinding said mixture until a solid-liquid slurry is produced, wherein: 1. said slurry is comprised of from 60 to 82 volume percent of solid carbonaceous material, from 18 to 40 volume percent of carrier liquid, and from 0.01 to 4.0 weight percent, by 25 weight of dry carbonaceous material, of dispersing agent; 2. said slurry has a yield stress of from 3 to 18 Pascals and a Brookfield viscosity at a solids content of 70 volume percent, ambient temperature, ambient pressure, and a shear rate of 100 revolutions per minute, of less than 5,000 30 centipoise; 3. the slurry consist has a specific surface area of from 0.8 to 4.0 square meters per cubic centimeter and an interstitial porosity of less than 20 volume percent; 4. from 5 to 70 volume percent of said particles of solid carbonaceous material are of colloidal size, being less than about 3 microns; , WIPO &?ΛTATlθ 5. said slurry comprises a consist of finely-divided particles of solid carbonaceous material, which consist has a particle size distribution substantially in accordance with the following formula: .vhere E J - 1.0 J-l J and vhere if D < and vhere if D > wherein: (a)CPFT is the cumulative percent of said solid material finer than a certain specified particle size D, in volume percent; (b)k is the number of component distributions in the consist and is at least 1; (c)X. is the fractional amount of the component j in the consist, is less than or equal to 1.0, and the sum of all the X 's in the consist is 1.0; (d)n is the distribution modulus of fraction j and is greater than 0.001; (e)D is the diameter of any particle in the consist and ranges from 0.05 to 1180 microns; (f)D is the diameter of the particle in fraction j, measured s at 1% CPFT, on a plot of CPFT versus size D, is less than D , and is greater than 0.05 microns; and (g)D.. is the diameter of the size modulus in fraction j, O PI j., WIPO -ZRNAΎ\ measured by sieve size or its equivalent, and is from 10 to 1180 microns. 17. The process as recited in claim 16, wherein said solid material is coke. 518. The process as recited in claim 17, wherein said solid carbonaceous material is petroleum coke. 19. The process as recited iα claim 16, wherein said solid carbonaceous material is coal. 20. The process as recited in claim 19, wherein said k is 1. lo 21. The process as recited in claim 20, wherein said carrier liquid is an alcohol containing from 1 to 10 carbon atoms. 22. The process as recited in claim 21, wherein said alcohol is selected from the group consisting of ethanol, ethanol, propanol, butanol, phenol, and mixtures thereof. 15 23. The process as recited in claim 20, wherein said carrier liquid is petroleum liquid. 24. The process as recited in claim 23, wherein said petroleum liquid is selected from the group consisting of number 2 fuel oil, number 4 fuel oil, number 6 fuel oil, gasoline, naphtha, and mixtures thereof. 20 25. The process as recited in claim 20, »wherein said carrier liquid is a mixture of water and petroleum liquid. 26. The process as recited in claim 25, wherein said carrier liquid is comprised of at least 90 weight percent of water and less than about 10 weight percent of petroleum liquid. 25 27. The process as recited in. claim 26, wherein said petroleum liquid is selected from the group consisting of number 2 fuel oil, nuber 4 fuel oil, number 6 fuel oil, gasoline, naphtha, and mixtures thereof. 28. The process as recited in claim 20, wherein said carrier liquid is 30 water. 29. The process as recited in claim 28, wherein: (a)the pH of said grinding mixture is from 7 to 11, (b)sald slurry has a yield stress of from 5 to 15 Pascals, and (c)the Brookfield viscosity of said slurry is less than 5 4,000 centipoise. 30. The process as recited in claim 29, wherein: (a)from 6 to 30 weight percent of the coal material in the grinding mixture has a median particle size of from 2 to 20 microns, and 10 (b)said grinding mixture is comprised of from 70 to 94 weight percent of coarse coal material which has a median particle size greater than 40 microns. 31. The process as recited in claim 30, wherein: (a)said slurry consist has an interstitial porosity of less than 15 15 volume percent and a specific surface area of from 0.8 to 3.0 square meters per cubic centimeter, and (b)the Brookfield viscosity of said slurry is less than 3,000 centipoise. 32. The process as recited in claim 31, wherein: 20 (a)said n is from 0.1 to 0.5, (b)said D_ J-l is from 30 to 420 microns, and (c)the Brookfield viscosity of said slurry is less than 2,000 -centipoise. 33. The process as recited in claim 32, wherein the colloidal sized " coal particles in said slurry have a net zeta potential of from 15 to 85 millivolts 34. The process as recited in claim 33, wherein said grindng mixture is ground in a tumbling mill. 35. The process as recited in claim 34, wherein said tumbling mill 30 is .a ball mill. 36. The process as recited in calim 35, wherein said grinding mixture is ground at from 50 to 70 percent of the ball mill critical speed. 37. The process as recited in claim 36, wherein said grinding mixture is ground at less than 60 percent of the ball mill critical speed. 38. The process as recited in claim 37, wherein the viscosity of said slurry is less than 1,000 centipoise.

Inventors: FUNK JAMES E, FUNK, JAMES, E.
Applicants: UNIV ALFRED RES, ALFRED UNIVERSITY RESEARCH FOUNDATION, INC.
Application year: 1984
Main classification: C10L1
IPC codes: C10L1, C10L10