A NOVEL CARBONACEOUS COMPACT, A SLURRY CONTAINING SAID COMPACT, AND A PROCESS FOR MAKING SAID SLURRY

Abstract: A grinding mixture with a pH of from 5-12 which contains about 60-82 volume percent of one or more carbonaceous materials, about 18-40 volume percent of one or more carrier liquids, and from about 0.01-4.0 weight percent of one or more dispersing agents. The mixture is comprised of at least two consists of carbonaceous material, one of which contains particles smaller than 53 microns. There is also disclosed a process for preparing a carbonaceous slurry comprising the steps of grinding the aforementioned grinding mixture until it contains a consist whose particles are in substantial accordance with a specified particle size distribution. The slurry produced by this process, and the compact in the slurry, also are described.

Description: Description A novel carbonaceous compact, a slurry containing said compact, and a process for making said slurry Technical Field My invention relates to a solids-liquid slurry which contains carbonaceous material and to a process for making such a slurry. The slurry contains at least 60 volume percent of solid material, has a relatively low viscosity and thus is pumpable, and can be burned directly in a furnace without removing liquid from it. Background Art The prior art teaches that high density coal-water . slurries have high viscosities and are substantially unpumpable. Thus, U.S. Patent - ,104,035 teaches that a coal-water slurry which contains about 50 percent of solids is unpumpable. Brief Description of the Drawings The present invention will be more fully understood by reference to the following detailed description hereof, when read in conjunction with the attached drawings, wherein like reference numbers refer to like elements and wherein: Fig. 1 is a flow sheet of a preferred process for preparing the slurry of this invention. Fig. 2 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. Disclosure of Invention In accordance with the present invention, I provide a coke compact comprising finely divided coke particles, characterized in that said coke compact comprises finely divided coke particles having a particle size in the range of 1180 microns to 0.05 microns, with from about 5 to about 70 volume percent of the coke particles being SU BSTITUTE SHEET smaller than about 3 microns, wherein said coke particles in said compact have a particle size distribution substantially in accordance with the following formula: It .vhere Σ !. E 1.0 5=1 3 and vhere if D < Ds-i D^j - and where if D > »Lj 1.0 ^ wherein: 1. CPFT is the cumulative percent of said coke material finer than a certain specified particle size D, in volume percent; 2. k is the number of component distributions in the compact, and is at least 1; 3. Xj. s the fractional amount of the component j in the compact, is less than or equal to 1.0, and the sun of all of the Xj's in the compact is 1.0; *l. 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 compact and ranges from about 0.05 to about 1 80 microns; 6. D s is the diameter of the smallest particle in fraction j, measured at ϊ% CPFT on a plot of CPFT versus size D, is less than DL, and is greater than 0.05 microns; 5 7. L is the diameter of the largest particle in fraction j, measured by sieve size or its equivalent, and is from about 15 to about 1180 microns; and 8. no more than about 0.05 volume percent 10 of the coke particles in the compact have a diameter less than about 0.05 microns. I also provide a coke-liquid slurry comprising a consist of finely-divided particles of coke dispersed 15 in said liquid, wherein: 1. said slurry is comprised of at least about 60 volume percent of said coke, less than about 40 volume percent of said liquid, and from about 0.01 to about 4.0 weight percent (based upon 20 the weight of dry coke) of dispersing agent; 2. said slurry has a yield stress of from about 3 to about 18 Pascals and a Brookfield viscosity at a solids content of 70 volume percent, ambient temperature, ambient pressure, and a shear rate 25 of 100 revolutions per minute of less than 5,000 centipoise; * .* 3« said consist has a specific surface area of from about 0.8 to about 4.0 square meters per cubic centimeter and an interstitial porosity of less 30 than 20 volume percent; 4. from about 5 to about 70 volume percent of said particles of coke are of colloidal size, being smaller than about 3 microns; 5. said consist of finely-divided particles of coke 35 has a particle size distribution substantially in accordance with the aforementioned CPFT formula; T TE SHEET \ 7 6. the net zeta potential of said colloidal particles of coke material is from about 15 to about 85 millivolts; and 7. the concentration of coke material in said slurry, the specific surface area of said consist, and the zeta potential of said colloidal size particles of solid carbonaceous material are interrelated in accordance with the following formula: 240 V„ + P β + SA + ZP H wherein: 1. V s is the percent, by volume, of coke material in said slurry; 2. . P is the porosity of said consist in the slurry, in percent; 3- S.A. is the specific surface area ' of said consist in said slurry, in square meters per cubic centimeter; 4. Z.P. is the net zeta potential of said colloidal size particles of carbonaceous material in said consist, in millivolts, and 5. H is from about 75 to about 98. In the aforementioned coke-liquid slurry, part of the coke material can be replaced by one or more other carbonaceous materials. When this occurs, then: (1) the total amount of carbonaceous material in the slurry (coke plus other carbonaceous material) is at least about; 60 volune percent; (2) from about 5 to about 70 volume percent of the particles of carbonaceous material in the slurry are of colloidal size; (3) the consist of finely divided particles of carbonaceous material has a particle size O distribution substantially in accordance with the aforementioned CPFT formula, wherein the terms of the formula refer to total carbonaceous material rather than just coke; (4) the net zeta potential of said colloidal 5 size particles of carbonaceous material is from about 15 to about 85 millivolts; and (5) in said "H equation", the term V s is the percent, by volume, of total carbonaceous material in the slurry. In summary, the same terms and conditions apply, with the exception that the 10 properties of the total carbonaceous solids in the slurry are substituted for the properties of the coke. I also provide a process for preparing a coke-liquid slurry comprising the steps of providing the aforementioned coke compact and mixing said compact with dispersing 15 agent and a sufficient amount of fluid to provide a suspension containing at least 60 volume percent of said coke and at least 18 volume percent of said fluid. I also provide a process for preparing a coke-liquid slurry comprising the steps of: (1) providing a coke-water 20 mixture which is comprised of from about 60 to about 82 volume percent of coke, from about 18 to about 40 volune percent of liquid, and from about 0.01 to about 4.0 percent, by weight of dry carbonaceous material, of dispersing agent; and (2) grinding said coke-fluid mixture 25 until the coke water slurry described above is obtained. , . • . I also provide a grinding mixture with a pH of from about 5 to about 12, wherein: (a) said mixture contains from about 60 to about 82 volume percent of solid carbonaceous material, from about 18 to about 40 volume 30 percent of carrier liquid, and from about 0.01 to about 4.0 weight percent, by weight of dry carbonaceous material, of dispersing agent; (b) said solid carbonaceous material in said mixture is comprised of at least one fine consist of solid carbonaceous material and at least one coarse 35 consist of solid carbonaceous material; and (c) at least about 5 weight percent of said solid carbonaceous material in said mixture is comprised of solid carbonaceous particles which are substantially all smaller than about 53 microns. I also provide a process for preparing a carbonaceous material-liquid slurry comprising the steps of (1) providing the aforementioned grinding mixture, and (2) grinding said mixture until a slurry with properties substantially identical to said coke-water slurry is obtained. The coke compact of the invention The compact of this invention is comprised of finely divided coke particles. The term "compact", as used in this specification, refers to a mass of finely-divided particles which are closely packed in accordance with this invention. Coke is the carbonaceous residue (70-80%) of a carbonaceous material (such as coal) after the volatile components have been distilled off. Thus, for example, coke is bituminous coal from hich the volatile constituents have been driven off by heat so that the fixed carbon and the ash are fused together. Any coke known to those skilled in the art can be used in the compact and/or the slurry of this invention. Thus, for example, one can use coke formed when bituminous coal is heated in either a limited air supply or in the absence of air. Petroleum coke, made from the fractionation of oil, also can be used in the compact and/or the slurry of this invention. Some of the coke in the compact of this invention can be replaced by one or more other carbonaceous materials. Alternatively, or additionally, mixtures of different cokes can be used in said compact. By way of illustration and not limitation, one can use a mixture of a coarse carbonaceous fraction and a fine carbonaceous fraction. As used in. this specification, the term "carbonaceous" refers to a carbon-containing material and includes, e.g., coal, coke, graphite, and the like. The coke compact of this invention is comprised of finely divided coke particles having a particle size in the range of from about 0.05 to about 1180 microns. It is preferred that, In the coke compact of this invention, at least 5 weight percent of the coke particles are smaller than about 3 microns. It is more preferred that from about 5 to about 70 weight percent of the coke particles in said compact be smaller than 3 microns. In one preferred embodiment, from about 5 to about 30 weight percent of the coke particles in said compact are smaller than 3 microns. In another preferred embodiment, from about 7 to about 20 weight percent of the coke particles in said compact are smaller than 3 microns. The particles in the compact of this invention have a particle size distribution which is in substantial accordance with the aforementioned CPFT formula. It is preferred that, in said formula: (1) k is from about 1 to about 30; (2) n is from about 0.001 to about 10.0, more preferably from about 0.01 to about 1.0, and most preferably from about 0.01 to about 0.5; and (3) DL is from about 30 to about 420 microns, and most preferably from about 100 to about 300 microns. In said CPFT formula, D s is the di-ameter of the smallest particle in fraction j (as measured by extra¬ polating the CPFT chart line, if necessary, to one percent CPFT using data from sieve analyses plus the Micro eritics Sedigraph 5500L). DL is the theoretical size modulus of the particle size distribution; when CPFT is plotted against size, the DL 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 coarse 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 DL 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 of this invention has a compact with a particle size distribution which is substantially in accordance with the CPFT equation; minor deviations caused by the actual top size being greater than the DL are within the scope and spirit of this invention. When k is 1, the aforementioned equation simplifies to: CPFT D n - us" 100 D^-D 8 when k is 2, the equation becomes: II wherein: X-j + X£ = 1.0 (i.e., the sum of the fractional parts is equal to the whole); when D is less than or equal to D S1 , the first term in the parentheses (term I) is equal to 0.0; when D is greater than or equal to DL.., the first term in the parentheses (term I) is equal to 1.0; when D is less than D 5 , the second term in the parentheses (term II) is equal to 0.0; when D is greater than DL_, the second term in the parentheses (term II) is equal to 1.0. The reason for the aforementioned constraints of the terms in parentheses I and II is that each of these terms refers to the equation of one of the two components. In order to sum the fractional parts of the two component distributions, the above considerations must be Included since the particles of a certain size may be represented between the effective D s and DL of the total distribution but not between the D s or DL of one of the component distributions. Thus, the values In parentheses I and II are subject to the limitations that, when D is less than or equal to D s , the value for the term is 0.0 and when D is greater than DL . the value of the term is 1.0. The equation given above for when k is 2 is simply the sum of two components where the fraction of component j is X and the fraction of component 2 is X2. Since, In this case, X* * and Xg make up the whole ' distribution, their sum must equal 1.0. In accordance with the above reasoning, when k = 3, the equation becomes: When.k = 4, there is a fourth term in the equation equal to: When k is 1 , it is preferred that D s be from about 0.05 to about 0.4 microns and , more preferably, from about 0.05 to about 0.25 microns, and, most preferably, from about 0.05 to about 0.20 microns. For any given compact, one can determine the particle size distribution by means well known to those skilled in the art. For measuring particle sizes and for determining particle size distributions of coke particles, the following two means can be used and are preferred: 1. U.S. Series sieves Nos. 16, 20, 30, 40, 50, 70, 100, 140, 200, 270, are used to determine weights of coke particles passing through each sieve in the range of about (-) 1180/jm to (-) 53 m. The cumulative volume percents of coke 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., Korcross, Ga., U.S.) is used to measure particle sizes and numbers of particles in coke and in the coke-fluid slurry in the range of (-) 75 wn to about 0.2 ran. The Sedigraph 5500L uses photo-extinction of settling particles dispersed in water according to Stoke's law as a means for making the above determinations. Other instruments, such as a Coulter Counter or combinations of the Leeds & orthrup Microtrac Particle Anaylzers 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 "D s at 1 " can be determined by extrapolating the CPFT chart line to this axis and reading the intercept. This number, although not the true D s can be effectively used in the computer- algorithm to determine % porosity and specific O surface area. In addition to the above methods, particle size measurements can be estimated from ethylene blue index measurements to obtain an approximate determination of the wgt. % of colloidal particles of size below I ran. 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. When the compact of this invention is mixed with carrier liquid, a solids-liquid slurry is produced which is comprised of a "consist". As used herein, and in the prior art, the term "consist" means the particle size distribution of the solid phase of the solids-liquid slurry. The compact of this invention has a specific surface area of from about 0.8 to about 4.0 square meters per cubic centimeter. Stated another way, when the compact of this invention Is used to prepare a solids-liquid slurry, said slurry has a consist with a specific surface area of from about 0.8 to about 4.0 square meters per cubic centimeter. It is preferred that said specific surface area to be from about 0.8 to about 3.0 m-^/cc. It is more preferred that the specific surface area be from about 0.8 to about 2.4 m^/cc. In an even more preferred embodiment, the specific surface area is from about 0.8 to about 2.0 m-^/cc. 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 particles in the consist are spherical, and then one calculates the surface area based on this assumption. Thus, once the particle size distribution of the consist is determined, it is assumed that each particle in the consist is spherical with a O surface area of D ; the όiameter 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 suπmed. The compact of this invention has an interstitial porosity of less than about 20 percent. Stated another way, when the compact of this invention is mixed with fluid to produce a slurry, said slurry is comprised of a consist with an Interstitial porosity of less than about 20 percent. It is preferred that said interstitial porosity be less than about 15 volume percent, and it is more preferred that said interstitial porosity be less than about 10 percent. The interstitial porosity is the total volume of the interstices of 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* (1 - [1/VAJ) where VA is as defined by the following modified Westman- Hugill algorithm: VA 3 = X l + X 2 + A 3 X 3 i-1 VA = E X + A.X. n-1 VA, = Σ X. + A X n j=i J n n OMPI wherein: Aj[ • = Apparent volume of a monodispersion of the ith si ze particle, Xi = Mass fraction of the i tn size particles, VAj = Apparent volume calculated with reference to the ikh size particles, n = Number of particle sizes, and VA = Maximum value of Vh = Apparent volume 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 the true porosity of a consist as measured, for example, by liquid loss due to the non-spherical morphology (shape) of the particles, and by invocation of D s at 1%. In the compact of this invention, no more than 0.05 volume percent of the coke particles in the slurry have a particle size less than 0.05 microns. It is preferred that at least 85 weight percent of the coke particles in the slurry have a particle size less than 300 microns. In the most preferred embodiment, at least 95 weight percent of the coke particles in the slurry have a particle size less than 300 microns. The coke slurry of this invention The coke slurry of this invention can be prepared by mixing the coke compact of this invention with carrier liquid and dispersing agent; when the compact is slurried, it is a "consist". The slurry of this invention contains at least about 60 volume percent of carbonaceous solids, by volume of slurry, measured on a dry basis. It is preferred that the slurry contain at least 70 volume percent of solids, dry basis; and it is more preferred that the slurry contain at least 80 volume percent of solids, dry basis. As used in this specification, the term "solids" refers to solid carbonaceous material (such as coke) which can include impurities. The term "dry basis" refers to coke which is substantially free of carrier liquid. Coke is considered to be 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 24 hours. The slurry of this invention is comprised of one or more liquids. As used in this specification, the term liquid refers to a substance which undergoes continuous deformation under a shearing stress. By way of illustration and not limitation, some of the liquids which can be used in the slurry of this invention includes water; waste industrial solvents such as, e.g., effluents from waste disposal plants, contaminated waste water containing hydrocarbons from e.g., oil- separation processes, and the like; aromatic and aliphatic alcohols containing 1-10 carbon atoms, such as methanol, ethanol, prσpanol, butanol, phenol and the like; pine oil; petroleum liquids such as, e.g., number 2 fuel oil, number 4 fuel oil, number 6 fuel oil, gasoline, naphtha, and the like; hydrocarbon solvents such as, e.g., benzene, toluene, xylene, kerosene, and derivatives thereof; acetone aniline; anisole; halobenzenes such as; e.g., bromobenzene and chlorobenzene; nitrobenzene; carbon tetrachloride; chloroform; cyclohexane; n-decane; dodecane; 1,1,2,2-tetrachloroethane; ethyl bromide, 1,2-dichloroethyIene; tetrachloroethylene; trichloroethylene; ethylene chloride; ethyl ether; ethyl iodide; glycol; n-hendecane; n-heptane; 1-heptanol; 1-hexanol, methylene halides such as, e.g., methylene chloride, methylene bromide, and methylene iodide; n-octadecane; n-octane; 1-octanol; n-pentadecane; pentanol; and the like. The 5 aforementioned list is merely illustrative. In one preferred embodiment, the liquid used in the slurry of this invention is carrier water. As used in this specification, the term "carrier water" means the bulk of free water dispersed between the coal particles 10 and contiguous to the bound layers on the particles, and it is to be distinguished from bound water. The 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, 15 pages 90-97 (at p. 91). Mixtures of two or more liquids can be used in the slurry of this invention. Thus, by way of illustration and not limitation, one may use mixtures of water and ethanol, water and oil, water and gasoline, and the 20like. One can use mixtures comprised of from about 1 to about 99 volume percent of alcohol and from about 99 to about 1 volume percent of water. In one preferred embodiment, the mixture is comprised of from about 1 to about 15 volume percent of alcohol with the remainder of 25 the liquid consisting essentially of water. It is preferred that the alcohol be liquid and monohydric and that it contain from about 1 to about 10 carbon atoms. Suitable monohydric alcohols are listed on page 265 of Fieser and Fieser's "Advanced Organic Chemistry" (Reinhold, N.Y., 301961), the disclosure of which is hereby incorporated by reference into this specification. The slurry of this invention preferably has a yield stress of from about 3 to about 18 Pascals. It is preferred that the yield stress be from about 5 to about 15 Pascals, 35and it is more preferred that the yield stress be from about 7 to about 12 Pascals. As is known to those skilled in 16 the art, the yield stress Is the stress which must be exceeded before flow starts. 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. See, for example, W. L. Wilkinson's "Non-Newtonian Fluids, Fluid Mechanics, Mixing and Heat Transfer" (Pergamon Press, New York 1960), pages 1-9, the disclosure of which is hereby incorporated herein by reference. Also see Richard W. Hanks, et al's "Slurry Pipeline Hydraulics and Design" (Pipeline Systems Incorporated, Orinda, California, 1980), pages II-1 to 11-10, the disclosure of which is also hereby incorporated herein by reference. The slurry of this invention has a relatively low viscosity even though it has a high solids content. The ' Brookfield viscosity of the slurry is tested after the solids concentration of the slurry is adjusted to a solids content of 70 volume percent (the slurry Is either diluted or concentrated until It has this concentration of solids), ambient temperature, ambient pressure, and a shear rate of 100 revolutions per minute. Under these test conditions, the viscosity of the slurry is less than about 5,000 centipoise. It is preferred that the viscosity of the slurry be less than about 4,000 centipoise. It is more preferred that the viscosity of the slurry be less than about 3»000 centipoise. In an even more preferred embodiment, the viscosity of the slurry Is less than about 2,000 centipoise. In the most preferred embodiment, the viscosity-of the slurry is less than about 1,000 centipoise. As used in this specification, the term- "Brookfield viscosity" describes viscosity as measured by conventional techniques by means of a Brookfleld Synchro-Lectric Viscosimeter (manufactured by the Brookfield Engineering Laboratory). The slurry of this invention contains a substantial amount of carbonaceous solid material(s) and less than about 40 volume percent (by volume of slurry) of liquid. It is preferred that the slurry contain less than about 30 volume percent of liquid. In the most preferred embodiment, the slurry contains less than about 20 volume percent liquid. The slurry of this invention contains from about 0.01 to about 4.0 weight percent of dispersing agent, based upon the weight of dry material. Means for determining the identity of the most effective dispersing agent for a given slurry will be described below for a coal water slurry, it being understood that the technique described is applicable to other slurries such as, e.g., coke-water, graphite-water, etc. In general, for any given slurry system, the identity of effective dispersing agents can be determined by measuring the effects of the dispersant upon the system at a given dispersant concentration; viscosity versus 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 slurry 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 slurry system under comparable concentration and test conditions. Thus, for example, one can dry grind a sample of coal in a laboratory size ball mill with porcelain or steel balls in water at 30 weight percent solids, e.g., for about 24 hours or until all of the particles in the coal are less than 10 microns in size; other grinding devices known to those skilled in the art may also be used such as vibroenergy mills, stirred ball mills, or fluid energy mills. Snail samples (about 500 milliliters apiece) of the slurry 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(s) concentration is the most effective for those conditions. This technique is described in detail in my U.S. Patent 4,282,006, the disclosure of which is hereby incorporated herein by reference. Figure 2 illustrates one means of evaluating the effectiveness of surfactants for any given solid material. The curves of Fig. 2 represent data obtained using both a purported nonionic polymer CW-11 m.ade 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 any candidate surfactant is 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 Fig. 2 the left ordinate gives the calculated zeta potential of the particles in millivolts, the right ordinate gives the specific conductance in micromhos per centi- 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 2 shows that the purported nonionic CW-11 surfactant does have some anionic character. CW-11 has a zeta potential of -50 mv at 300% addition 0.01% dry coal. Polyfon-F has a zeta potential of -55 mv at 200% addition on 0.01% dry coal. Furthermore the specific conductance of the Polyfon-F at -55 mv zeta potential is greater than CW-11 at -50 mv. These data establish Polyfon-F as a more chemically effective surfactant for use on this particular Australian coal. The amount of dispersing agents used will vary, depending upon such factors as the concentration of the coke in the slurry, the particle size and particle size distribution, the temperature of the slurry, the pHj the original zeta potential of the particles, and the identity of the dispersing agent(s) and its concentration. In general, the dispersing agent is present in the slurry, at from 0.01 to 4.0 weight percent based on the weight of dry coke. Procedurally, in determining the amount of a specific dispersing agent needed, a series of measurements can be made of viscosities versus shear rates versus zeta potential for a series of solids-liquid slurries containing a range of amounts of a particular dispersing agent for a constant amount of solids-liquid slurry. The data can be plotted and used as a guide to the optimum quantities of that agent to use to obtain near maximum or maximum zeta potential for that slurry system. The coordinate of the chart at which the viscosity and/or zeta potential is not changed significantly by adding more agent is selected as an indication of the optimum quantity at maximum zeta potential, and the amount is read from the base line of the chart. The viscosity and amount read from the titration chart is then compared with an equivalent chart showing a correlation among viscosity, amount, and maximum zeta potential. An amount of electrolyte and/or dispersing agent(s) required to provide a maximum or near maximum zeta potential and a selected viscosity can then be used to make solids-liquid slurry. It is preferred that the slurry of this invention be comprised of an amount of dispersing agent effective to maintain the particles of material in dispersed form in the carrier liquid of the slurry, to generate a yield stress in the slurry of from about 3 to about 18 Pascals, and to charge the colloidal coke particles in the slurry to a net zeta potential of from about 15 to about 85 millivolts. It is preferred that the slurry of this invention contain from about 0.01 to about 4.0 percent, based on weight of dry solids, of at least one dispersing agent. It is more preferred that the slurry contain from about 0.03 to about 1.8 percent, based on weight of dry solids, of dispersing agent. In an even more preferred embodiment, the slurry contains from about 0.05 to about 1.4 percent, by weight of dry solids, of dispersing agent. In the most preferred embodiment, the slurry contains from about 0.10 to abut 1.2 percent of dispersing agent. Any dispersing agent which disperses the coke particles in the liquid and imparts the specified yield stress and zeta potential values to the slurry can be used. As is known to those skilled in the art, the dispersing agent can be inorganic. The dispersing agent can be, and preferably is, organic, i.e., it contains carbon. The dispersing agent is preferably an anionic organic surfactant. It is preferred that the dispersing agent used in the slurry of this Invention be an organic compound which encompasses in the same molecule two dissimilar structural groups, e.g., a water soluble moiety, and a water insoluble moiety. It is preferred that said dispersing agent be a surfactant. The term "surface-active agent", or "surfactant", as used in the prior art indicates any substance that alters energy relationships at interfaces, and, in particular, a synthetic or natural organic compound displaying surface activity including wetting agents, detergents, penetrants, spreaders, dispersing agents, foaming agents, etc. Q1. The surfactant used in the slurry of this invention is preferably an organic surfactant selected from the group consisting of anionic surfactants, cationic surfactant, and amphoteric surfactants. It is preferred that the surfactant be either anionic or cationic. In the most preferred embodiment, the surfactant is anionic. It is preferred that the molecular weight of the surfactant used in the slurry of this invention be at least about 200. As used herein, the term "molecular weight" refers to the sum of the atomic weights of all the atoms in a molecule. In one preferred embodiment, the surfactant is anionic 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 anionic surfactants is a polyacrylate. In another preferred embodiment, the surfactant is cationic and its solubilizing group(s) is selected from the group consisting of a primary amine group, a secondary amine group, a tertiary amine group, a quaternary ammonium group and mixtures thereof. In yet another embodiment, the surfactant is amphoteric. In this embodiment, the surfactant has at least one solubilizing group selected from the group consisting of a carboxylate group, a sulfonate group, a sulfate group, a phosphate group, and mixtures thereof; and the surfactant also has at least one solubilizing group selected from the group consisting of a primary amine group, a secondary amine group, a tertiary amine group, a quaternary a moniun group, and mixtures thereof. By way of illustration and not limitation, some suitable surfactants include the alkali metal salts of a condensed mono-naphthalene sulfonic acid. This surfactant, whose preparation is described in U.S. Patent 3,067,243 (the disclosure of which is hereby incorporated by - reference into this specification), can be prepared by 22 sulfonating naphthalene with sulfuric acid, condensing the sulfonated naphthalene with formaldehyde, and then neutralizing the condensate so obtained with sodium hydroxide. This alkali or NHi|+ metal salt of a condensed mono-naphthalene sulfonic acid is comprised of at least about 85 weight percent of a repeating structural unit of the formula: wherein M Is an alkali metal selected from the group consisting of sodium, potassium, and ammonium and a is an integer of from 1 to 8. Comparable compounds with a benzene rather than naphthalene nucleus also can be used. Some other illustratively suitable surfactants which can be used include, e.g., the sodium salt of a carboxylated polyelectrolyte sold under the tradename of "Daxad" by the W.R. Grace and Co.; the sodium salt of condensed mono naphthalene sulfonic acid sold under the name of "Lomar D" by the Diamond Shamrock Process Chemicals, Inc., "Nopcosperse-VFG", a condensed alkyl naphthalene sulfonate sold by the Diamond Shamrock Co.; Darvan #1, # and #6, polymerized benzene sulfonates solid by R.T. Vanderbilt, Inc.; alkyl aryl sulfonates such as "Texo LP583" (sold by the Texo Corporation) and "Petro 424LS" (sold by the Petro Chemicals Co.); lignosulfonates; and the like. The preferred lignosulfonates 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 50 phenyl propane units), and are made up of cross-linked polyaromatic chains. Some of the preferred lignosulfonates include those listed on page 293 of McCutcheon's "Bnulsifiers and Detergents), North American Edition (McCutcheon Division, MC Publishing Co., Glen Rock, N.J., 1981) and in the other portions of McCutcheon's which describes said lignosulfonates, the disclosure of which is hereby incorporated by reference into this specification. In one preferred embodiment, the lignosulfonate surfactant contains from about 0.5 to about 8.0 sulfonate groups. In one embodiment, the dispersing agent used in the slurry of this invention is a polyelectrolyte which, preferably, is organic. As used in this specification, the term "polyelectrolyte" indicates a polymer 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, or phosphate groups. Suitable polyelectrolytes include, e.g., the alkali metal and aπmonium salts of polycarboxylic acids such as, for instance, polyacrylic acid; the sodium salt of condensed naphthalene sulfonic acid; polyacrylamide; and the like. In one preferred embodiment, the slurry of this invention also contains from about 0.05 to about 4.0 weight percent by weight of dry solids in the slurry, of an electrolyte which, preferably, is organic. As used in this specification, the term "electrolyte" refers to a substance that dissociates into two or more ions to some extent in water or other polar solvent. This substance can be, e.g., an acid, base or salt. In a more preferred embodiment, the slurry of this invention is comprised of from about 0.05 to about 2.0 weight percent of an inorganic electrolyte. In the preferred embodiment, said coal-water slurry is comprised of from about 0.1 to about 0.8 weight percent of said electrolyte. In the most preferred embodiment, the slurry contains from about 0.1 to about 0.5 percent of inorganic electrolyte. Any of the inorganic electrolytes known to those skilled in the art can be used in the slurry of this invention. Thus, by way of illustration and not limitation, one can use the ammonia or alkali metal salt of hexa etaphosphates, pyrophosphates, sulfates, carbonates, hydroxides, and halldes. Alkaline earth metal hydroxides can be used. Other inorganic electrolytes known to those skilled in the art also can be used. It Is preferred that the slurry of this invention contain both said dispersing agent(s) and said inorganic electrolyte(s) and that from about 0.05 to about 10.0 parts (by weight) of the inorganic electrolyte are present for each part (by weight) of the dispersing agent(s) in the slurry. It is preferred that the total concentration of both the dispersing agent(s) and/or the inorganic electrolyte be from 0.05 to 4.0 weight percent. The coke consist used in the slurry of this invention is comprised of at least about 5 weight percent of colloidal particles. As used herein, the term colloid refers to a substance of which at least one component is subdivided physically is 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 classified as colloids. See Encyclopedia of Chemistry, 2d Edition, Clark et al (Reinhold, 1966), page 203, the disclosure of which is hereby incorporated herein by reference. It is preferred that the colloidal sized particles of coke in the coke-liquid slurry have a net zeta potential of from about 15 to about 85 millivolts. As used herein, the term "zeta potential" refers to the net potential, be it positive or negative in charge; thus, a zeta potential of from about 15.4 to 70.2 millivolts includes zeta potentials of from about -15.4 to about -70.2 millivolts as well as zeta potentials of from about +15.4 to about +70.2 millivolts. In a more preferred embodiment, said zeta potential is from about 30 to 70 millivolts. As used in this specification, the term "zeta potential" has the meaning given it in the field of colloid chemistry. Concise discussions and descriptions of zeta potential and methods for its measurement are found in many sources including, U.S. Patents 3,454,487 and 3,976,582, the Encyclopedia of Chemistry, 2d Edition, Clark et al., Reinhold Publ. Corp. 1966, pages 263-265; Chemical and Process Technology Encyclopedia, D.M. Considine, editor- in-chief, McGraw-Hill Book Company, N.Y., pages 308-309. "Zeta potential" may be measured by conventional techniques and apparatus of electroosmosis, such as those described, e.g., in Potter, "Electro Chemistry", EET Cleave -Hume Press, Ltd., London (1961). Zeta potential can also be determined by measuring electrophoretic mobility (EPM) in any of several commercial apparatuses. A Pen Kern System 3000 (made by Pen Kern Co., Inc. of Bedford Hills, N.Y.) can be used for determining zeta potential. 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 um sized coal particles in the coke compact of the coke-water slurry. It is preferred that the zeta potential of the colloidal sized coke particles in the coke consist of the slurry of this invention be negative in charge and be from about -15.4 to about -70.2 millivolts. It is more preferred that said zeta potential be from about -30 to about -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 solids 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. Snail samples of this larger sample can then be 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 coke-water slurry. Various acidic and basic salts are then added in incremental amounts to vary the pH, and various concentrations of various candidate dispersing agent organic surfactants likewise are added in incremental amounts (e.g., grams per gram coal, both dry basis), alone or in combinations of two or more. These samples are then evaluated in any electrophoretic mobility, electroosmosis, or streaming potential apparatus to determine electrical data-, from which the zeta potential is calculated in a O 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 coke particles in the carrier liquid below the amount at which dilatancy may be reached. In the coke slurry of this invention, the concentration of the carbonaceous material in the slurry (coke and any other carbonaceous material present, referred to as "V s ", the interstitial porosity of the slurry consist (P s ), the specific surface area of the slurry consist (S.A.), and the zeta potential of the colloidal sized particles of carbonaceous material in the slurry (colloidal coke and any other colloidal carbonaceous material present) are interrelated in accordance with the "H equation" described above. In one preferred embodiment, the only carbonaceous material in the slurry consist is coke. The mixing process of this invention In the mixing process of this invention, the coke slurry of this invention is produced by mixing the coke compact of this invention with carrier liquid and dispersing agent. From about 60 to about 80 volume percent of at least one coke solid is mixed with carrier liquid and surfactant. The terms "mixed" and "mixing", as used in this specification, refers to the steps of combining or blending several masses into one mass and includes, e.g., 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 the process of this invention. Thus, by way of illustration and not limitation, one can use batch mixers such as change-can mixers, stationary tank mixers, gate mixers, shear-bar mixers, helical blade mixers, double-arm kneading mixers, screw-discharge batch mixers, intensive mixers, roll mills, bulk blenders, Littleford- Lodige mixers, cone and screw mixers, pan muller mixers, OM / VIP and the like; one can use continuous mixers such as single-screw extruders, the Rietz extrudor, the Baker Perkins Ko-Kneader, the Transfer-Mix, the Baker Perkins Rotofeed, twin-screw continuous mixers, trough and screw mixers, pug mills, the Kneadermaster, and the like; one can use tumbling mills such as, e.g., ball mills, pebble mills, rod mills, tube mills, compartment mills, and the like; and one can use non-rotary ball or bead mills such as stirred mills including the Sweco dispersion mill the Attritor, the Bureau of Mines mill described in U.S. Patent 3,075,710, vibratory mills such as the Vibro-Energy mill, the Podmore Boulton mill, the Vibrato , and the like. The various processes and apparatuses which can be used to mix the carbonaceous solid with the carrier liquid and dispersant are well known to those skilled In the art and are described in, e.g., Perry and Chilton's Chemical Engineer's Handbook, Fifth Edition (MsGraw Hill, New York, 1973), pages 19-14 to 19-26 (Paste and viscous-material mixing), and 8-16 to 8-44 (crushing and grinding equipment). The disclosure of the aforementioned portions of the Chemical Engineer's Handbook is hereby incorporated by reference into this specification. When the liquid mixed with the carbonaceous solid is water or is comprised of from about 5 to about 99 weight percent of water, it is preferred that the temperature of the solids-liquid mixture be maintained at from ambient to about 99 degrees centigrade to insure that the water does not substantially vaporize; thus, if need be, said mixture can be cooled by conventional means during the mixing step. From about 60 to 82 volume percent of at least one carbonaceous solid is mixed with liquid and dispersing agent in the process of this invention. It is preferred to use from about 63 to about 77 volume percent of at least one solid carbonaceous material in said process, and it is more preferred to use from about 66 to about 73 volume percent of said solid material. The carbonaceous solid can be comprised of one or more fractions of carbonaceous material. Thus, with reference to coke, e.g., the carbonaceous solid used in the process of this invention can be (1) one coke consist, or (2) a blend of several different coke consists. In one preferred embodiment, at least two consists of carbonaceous solid material are mixed with liquid. In this embodiment, (1) both of the consists can be dry ground and mixed with liquid and dispersant, (2) the dispersant can be mixed with the liquid, and the dry ground consists can be mixed with 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 the liquid 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 consist can be wet ground with no dispersant and insufficient total water and then blended with dispersant and the balance of the water and/or other consist blends. In the process of this invention, the carbonaceous solid material is mixed wiht dispersant and from about 18 to about 40 volume percent of liquid. It is preferred to mix the solid with no more than about 30 volume percent of said liquid. It is even more preferred to mix the solid with no more than 25 volume percent of said liquid. The grinding process of this invention In the grinding process of this invention, a coke-fluid slurry comprised of from about 60 to about 82 volume percent of coke, from about 18 to about 40 volume percent of carrier liquid, and from about 0.01 to about 4.0 weight O .A,. YIP percent of dispersing agent is ground until (1) the slurry consist contains at least about 5 weight percent of colloidal coke particles, (2) the particle size distribution of the slurry consist is in substantial 5 accordance with the aforementioned CPFT formula, (3) the concentration of coke material in the slurry, the interstitial porosity of the consist, the specific surface area of the consist, and the zeta potential of the colloidal particles of carbonaceous material in the 10consist are interrelated in accordance with said "H equation"; and (4) preferably, the Brookfield viscosity of the slurry when tested under ambient conditions and at 100 RPM is less than 5,000 centipoise. In one preferred embodiment of the grinding process 15of this invention, the grinding is conducted in either a tumbling mill arid/or a non-rotary ball or bad mill selected from the group consisting of ball mills and stirred ball mills. When a ball mill is used to grind the mixture, it is preferred that the ball mill be run 20at a reduced speed. In this embodiment, the mixture is ground at said high solids content of from about 66 to about 77 volune percent of coke and at a ball mill speed of from about 50 to about 70 percent of the ball mill critical speed. The critical speed of the ball mill is 25the theoretical speed at which the centrifugal force on a ball in contact with the mill shell at the height of its • path equals the force on it due to gravity, and it is defined by the equation: 76.6 Nc =— W 30wherein N c is the critical speed (in RPM), and D is the diameter of the mill (feet) for a ball diameter that is small with respect to the mill diameter. A description of tumbling mills, such as ball mills, appears on pages 8-25 to 8-29 of the Fifth Edition of the Chemical Engineer's Handbook (edited by Perry and Chilton, McGraw Hill, New York, 1973). The grinding mixture of this invention The novel grinding mixture of this invention has a 5 pH of from about 5 to about 12 and, preferably, from about 7 to about 11. Said mixture contains at least about 60 volume percent of carbonaceous solid material, such as coke and/or coai, although it is preferred that the mixture contain at least 70 volume percent of solid carbonaceous material; 10 in the most preferred embodiment, the mixture contains at least about 80 volume percent of solid carbonaceous material. The mixture also contains from about 18 to about 40 volume percent of carrier liquid and from about 0.01 to about 154.0 weight percent, by weight of dry carbonaceous material in the mixture, of dispersing agent. There are at least two consists of carbonaceous solid material in the grinding mixture. There is at least one fine consist of material, and at least one coarse 20 consist of said material. The fine consist of carbonaceous solid material is comprised of solid carbonaceous particles which are substantially all smaller than 53 microns; at least about 99.5 weight percent of the carbonaceous particles in the fine consist are smaller than 53 microns. At least 55 weight percent of the solid carbonaceous particles in the grinding mixture are smaller than 53 microns. It is • preferred that from about 5 to about 20 weight percent of the solid carbonaceous particles in the grinding mixture be smaller than 53 microns. 0 The fines addition - high solids grinding process of this invention . - In one of the preferred processes of this invention, the grinding mixture of this invention is ground until: (1) the slurry consist contains at least about 5 weight 5 percent of colloidal carbonaceous particles; (2) the particle size distribution of the slurry consist is in substantial accordance with the aforementioned CPFT formula; (3) the UB S TITUTE SHEET S concentration of carbonaceous material in the slurry, the interstitial porosity of the consist, the specific surface area of the consist, and the zeta potential of the colloidal particles of carbonaceous material in the consist are interrelated in accordance with said "H equation", and (4) preferably, the Brookfield viscosity of the slurry, when tested under ambient conditions and at 100 RPM, is less than 5,000 centipoise. Illustration of the process of this invention 10 Several typical means of practicing the process of applicant's invention are illustrated in Fig. 1. The process of Fig. 1 will be described with reference to coal, it being understood that said process is generally equally applicable for use with other carbonaceous 15materials, such as, e.g., coke. In a wet grinding method, coal is charged to crusher 10. Any of the crushers known to those skilled in the art to be useful for crushing coal can be used as crusher 10. Thus, by way of Illustration, one can use, e.g., a 20rod mill, a gyratory crusher, a roll crusher, a jaw crusher, a cage mill, and the like. Generally, the coal Is crushed to a size of about 1/4" x 0, although coarser and finer fractions can be used. The crushed coal is fed through line 12 to mill 2514. Mill 14 can be either a tumbling mill (such as a ball mill, pebble mill, rod mill, tube mill, or compartment mill) or a non-rotary ball or bead mill. Liquid (such as water) and diluted dispersing agent are fed through lines 16 and 18, respectively, to mill 14. 30 The mill 14 will have sufficient coal and liquid fed to It so that it will contain from about 60 to about 82 volume percent of coal. Generally, one should charge from about 0 to about 10 volume percent more coal to mill 14 than he desires in the final slurry product. 35 In general, less than about 40 volume percent of liquid and from about 0.01 to about 4.0 weight percent of dispersant (based on weight of dry coal) will be fed in lines 16 and 18, respectively, to mill 14. When mill 14 is a ball mill, it is preferred to run it at less than about 70 percent of its critical speed. It is more preferred to run ball mill 14 at 5 about 60 percent of its critical speed. It is more preferred to run ball mill 14 at less than about 55 percent of its critical speed. In one of the most :.- preferred embodiments, ball mill 14 is run at less than about 52 percent of its critical speed. 10 Ground slurry from mill 14 is passed through line 20 through sieve 22. Sieve 22 may be 40 mesh sieve which allows underflow slurry of sufficient fineness (less than 420 microns) through to line 24; overflow particles which are greater than 420 microns are recycled 15 via line 26 back into mill 14 wherein they are subjected to further grinding. A portion of the underflow slurry from line 24 flows through line 28, visco eter 30, density meter 32, and particle size distribution analyzer 34; the remaining 20 portion of the underflow slurry flows through line 36. Any of the viscometers known to those skilled in the art can be used as viscometer 30. Thus, by way of illustration, one can use a Nametre Viscometer. The viscometer 30 indicates the viscosity of the ground 25 slurry. If the viscosity of the ground slurry is higher than desired, then either mill 14 is not grinding the coal to produce a sufficiently high surface area, and low porosity, and/or the amount or type of dispersing agent used is insufficient to produce a sufficiently high zeta 30 potential on the colloidal coal particles; and the underflow slurry should be subjected to further tests (in density meter 32 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 3532 indicates the density of the underflow slurry, which directly varies with its solids content. If the density of the underflow slurry is lower or higher than desired, then it is possible that the particle size distribution of the coal compact in the underflow slurry is lower or higher than desired. In this case, the underflow slurry should be subjected to further tests, in particle size 5 analyzer 3 to determine what the particle size distribution of the underflow slurry Is and its attendant surface area and porosity. Particle size distribution analyzer 34 analyzes the particle size distribution of the compact of the 10 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 analyzer 1534 the specific surface area and the porosity of the compact of underflow slurry can be determined. If the solids content, the viscosity, the specific surface area, and the porosity properties of the underflow slurry are as desired, then the underflow slurry is passed 20 through line 38 to final trim tank 40. If, however, either the solids content, the viscosity, the specific surface area, or the porosity property of the underflow slurry is not as desired, then a portion of underflow slurry is passed through line 36 to mill 42. Depending on how 25 badly the underflow slurry is out of specification, from about 1 to about 30 volume percent of the underflow slurry • is passed to mill 42 and the remainder is passed to trim tank 40. Recycling the slurry to mill 42 and, after regrinding, to mill 14, increases the quality of the slurry 0 coming out of mill 14. Mill 42 can be either a tumbling mill (such as a ball mill) or a non-rotary ball or bead mill (such as a stirred ball mill). When mill 24 is a tumbling ball mill, it is preferred to run it at less than about 70 percent of its 5 critical speed and, more preferably, at less than about 60 percent of its critical speed; in the most preferred embodiment it is run at O τ ' less than about 55 percent of its critical speed. Water is fed into mill 42 through line 44 so that the solids concentration of the ground slurry fed through line 36 will be adjusted to about 30 to about 60 volume 5 percent. The diluted slurry in mill 42 is then ground in mill 42 until at least about 95 volume percent of the particles in the slurry have diameters less than about 20 microns. It Is preferred to grind the slurry in mill 42 until at least 95 volume percent of the particles in 10the slurry are smaller than 15 microns and, more preferably, 10 microns. In the most preferred embodiment, the diluted slurry in mill 42 is ground until at least about 95 volume percent of the particles in the slurry have diameters less than about 5 microns. 15 The slurry ground in mill 42 is then passed through line 46 to high shear mixer 48. Any of the high-shear, high-intensity mixers known to those skilled in the art can be used as mixer 48; thus, e.g., the mixers described on page 19-7 of Perry and Chiton's Chemical Engineer's 20Handbook, Fifth Edition, supra, can be used. Dispersing agent is passed through line 50 to high shear mixer 48 in order to optimize the zeta potential of the colloidal particles in the slurry. For a given coke, . dispersant, and solids content a given amount of dispersant 25 will optimize zeta potential, and this amount can be determined in accordance with the screening tests described in this specification. From about 70 to about 110 percent of the amount of dispersant required to obtain the maximum zeta potential should be charged through line 3050 to mixer 48. In general, the ground slurry is inixed with water and dispersant in mixer 48 for from about 3 to about 15 minutes and, preferably, for about 10 minutes. The mixture from mixer 48 to then passed through line 52 and 5through viscometer 54, density meter 56, and particle size distribution analyzer 48. If the properties of the mixed slurry from mixer 48 are not suitable, then the water flow to mill 42 through line 44 and/or the slurry flow to mill 42 through line 36 and/or the dispersant flow to mixer 48 through line 50 are adjusted until the properties are suitable. If the properties of the mixed slurry from mixer 5 48 are suitable, then the mixed slurry is reycled to trim tank 40 or to mill 14 through line 60 where it is mixed with and ground with crushed coal from line 12, water from line 16, and dispersant from line 18. Figure 1 also illsutrates a dry grinding process 10 for making the stabilized slurry of this invention. In this alternative process, crushed solid material, such as coke, from crusher 10 is passed through line 62 to dry grind 64, where it is dry ground. Any dry grinder known to those skilled in the art can be used. Thus, by way of 15 example, one can 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, Fifth Edition, supra. The crushed material is ground in grinder 64 until it is pulverized, that is until it is a consist of about 2040 mesh x 0. The ground carbonaceous material from dry grinder 64 is passed through line 66 to trim tank 40. Water and dispersing agent are passed through lines 68 and 70, respectively, to trim tank 40. The carbonaceous 25 aterial/water/dispersant mixture is stirred by stirrer 72, and the stirred mixture is passed through ' line 74 to high shear mixer 76. Any of the high-shear mixers described above can be used as mixer 76. The quality of the slurry produced in mixer 76 is evaluated 0 by passing it through line 78 to zeta potential analyzer 80, particle size distribution analyzer 82, Haake viscometer 84, (for measuring yield stress), and density meter 86. If the net zeta potential of the colloidal particles in the slurry is from about 10 to about 90 5 millivolts, the solids content is from about 60 to 82 volume percent, the yield stress is from about 3 " - to about 18 Pascals, the surface area is from about 0.8 to about 4 m 2 /cc, the porosity is less than 20 volume percent, and the compact in the slurry is described by the aforementioned equations, then the slurry produced by the dry grinding is satisfactory. However, if the slurry is not up to . specifications, then a portion of the ground coal from line 66 is passed through line 86 to be dry ground in a micronizer fluid energy (jet) mill. The fine particles from jet mill 88 are passed through line 90 to trim tank 40 where they are mixed with the ground coal from line 66, the water from line 68, and the dispersant from line 70. Thereafter, the slurry produced in trim tank 40 is again evaluated in zeta potential analyzer 80, particle size distribution analyzer 82, Haake viscometer 84, and density meter 85 to determine whether the slurry is up to specifications. The process can be fine-tuned by this method until the properties of the slurry are as required; alternatively or additionally, one can alter the rate of flow of water and surfactant through lines 68 and 70, respectively, the rate of flow of coal from line 66 (by varying the speed of the mill and/or the rate at which crushed coal is fed to the mill through line 62), and the like. Alternatively, ground coal from dry grinders can be fed directly back to mills 14 or 42 and as feed for the wet grinding circuits. In yet another method illustrated in Fig. 1, the amount of very finely ground slurry material in trim tank 40 can be increased by passing a portion of the mixed slurry from high speed mixer 48 through line 92 into trim tank 40. Alternatively, or additionally, the amount of moderately finely ground slurry material in trim tank 40 can be increased by passing a portion of the ground slurry from ball mill 14 through line 38 to slurry tank 40. This scheme allows various fractions of slurries from wet grinders 14 and 42 to be blended with various fractions of dry consist from dry grinders 64 and 88. The following examples are presented to illustrate the claimed invention but are not to be deemed limitative thereof. Unless otherwise stated, all parts are by weight and all temperatures are in degrees centigrade. Example 1 - Procedure for screening and selecting dispersing . agent A surfactant or combination of surfactants effective for use in practicing the invention may be found by either of the two following methods. (a) Zeta potential measurement In general, a sample of carbonaceous material is ground in a laboratory size porcelain ball mill with porcelain balls in water at 30 wgt. % solids for approximately 24 hours to insure that all the particles are < IOJLBΠ. Sπ.all samples of this larger sample are then 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. Various acidic and basic salts are then added in incremental amounts to vary the pH, and various concentrations of various candidate dispersing agent organic surfactants likewise are added to incremental amounts (e.g. grams per gram coal, both dry basis), alone or in combinations of two or more. These samples are then evaluated in any electrophoretic mobility, electrosomosis, or streaming potential apparatus to measure electrical potentials, from which the zeta potential is calculated in a known way. Plots of zeta potential vs pH vs concentration may then be made to indicate candidate surfactants, or combinations thereof to be used to produce the optimum dispersion of particles in the carrier water below the amount at which dilatancy may be reached. A Pen Kern System 3000 apparatus is used in the determination described and can process 40 samples in about 6 hours. (b) Alternate method for estimating equivalent zeta potential A large sample of the material is ground in water as described in (a) above at 50 wgt. % solids for about 2 to 4 hours to produce a slurry. Smaller samples, about 500 ml, of this slurry are then deflocculated by adding various candidate dispersing agent surfactants and surfactant combinations to the sample of slurry, as above, dry or, preferably, in solution, dropwise, blending gently, and then measuring the viscosity at some constant shear rate (e.g., using a Brookfield LVT viscometer at 30 RPM). A surfactant system which is found to produce an acceptably low, preferably the lowest, viscosity at the lowest amount, e.g. in wgt. % of addition on a dry coal basis is thereby identified as the most effective surfactant. Example 2 - Preparation of samples for measurements (a) Sieve analysis Although any standard procedure may be used to measure particle sizes of carbonaceous particles and then to calculate the particle size distribution, the procedure used in obtaining data discussed herein will be described. A weighed sample, e.g. 50 grams dry wgt. of the material is dispersed in 400 ml of carrier water containing 1.0 wgt. % Lomar D based on a weight of material, dry basis, and the slurry is mixed for 10 minutes with a Hamilton Beach mixer. The sample is then allowed to stand quiescent for 4 hours, or preferably, overnight. (This step usually is not necessary if the slurry was milled with surfactant). The sample is then remixed very briefly. It then is poured slowly on a stack of U.S. Standard sieves over a large vessel. The sample is carefully washed with running water through the top sieve with the rest of the stack intact until all sievable material on that sieve is washed through the sieve into the underlying sieves. The top sieve is then removed and each sieve in the stack, as it becomes the top sieve, is successively washed and removed until each sieve has T been washed. The sieves are then dried in a dryer at 105°C and the residue on each is weighed in a known way. (b) Sedigraph analysis A separate sample finer than 140 mesh sieve size is carefully stirred and a representative sample (about 200 ml) is taken for analysis. The rest may be discarded. About 2 eyedroppers of the dilute slurry are further diluted in 30 ml of distilled water with 4 drops of Lomar D or other effective dispersant added. This sample is stirred overnight with a magnetic stirrer. Measurement is then made with the Sedigraph 5500L. The Sedigraph 5500L uses photo extinction to measure particles. It essentially measures projected area of shadows and the data must be converted to volume-%-finer- than any given particle diameter. The data from the sieve and Sedigraph is combined to prepare a CPFT chart. D s at 1% is read from the CPFT line. Example 3 - Preparation of coke/water slurry In this example, samples of petroleum coke from an oil refinery in MacPherson, Kansas were used as feedstock for a 16" Abbe ball mill. This coke material had a very high carbon content, low ash content, and low volatile residue remaining from the fractionation of crude oil. The ball mill used in this example was model Double No. 2, manufactured by the Paul 0. Abbe Company of Little Falls, New Jersey.. The ball charge in the mill was a 2-inch top Bond ball charge, containing 34% by weight 2-inch balls, 43% by weight 1.5-inch balls, 17% by weight 1.25 inch balls, and 6% by weight of 1.0 inch balls. The ball charge loading was 34% of the mill volume. The ball mill was run at a mill speed of 34 RPM or 51% of its critical, speed. The petroleun coke was first crushed to a 4 x 0 mesh consist in a roll crusher. Thereafter, in each of the experiments described in the Table 1 presented below, 16.3 pounds of the crushed petroleun coke was ' mixed with varying amounts of water, LomarΦϋ , (the sodium salt of condensed mono naphthalene sulfonic acid, sold by the Diamond Shamrock Process Chemicals Co.), and caustic to form grinding mixtures which each contained at least about 73 weight percent of coke solids. Table 1 indicates the concentration of the coke in each of the grinding mixtures ("weight % solids"), the concentrations of LomarvD and caustic in each of the grinding mixtures, the amount of the slurry consist produced which was smaller than 50 mesh and 200 mesh (weight percent), and, in some cases, the specific surface area, the interstitial porosity, and the-Bingham viscosity of the slurries produced. ET 42 Table 1 Grinding Conditions Product Slurry Weight Lomar D NaOH %<50 M *<200M - S.A. Poros. Bingham % solids % % m 2 /cm3 % Viscos. cP 73 0.7 0.1 99.25 67.99 75 0.7 0.1 99.49 69.36 1.01 6.53 78 0.7 0.1 99.69 72.07 1.54 7.87 810@75% 78 0.5 0.1 99.16 66.67 1.31 6.50 900§75% 78 0.7 0.1 99.02 70.64 1.61 5.42 78 0.7 0.05 99.37 69.99 74.5 0.7 0i15 99.98 84.98 1.80 8.47 Example 4 - Preparation of coal/water slurry Three hundred thirty-five pounds of 4 x 0 Ohio Ho. 6 bituminous coal with a Hardgrove grindability index (HGI) of 50 and a free swelling index (FSI) of 3.5, 6.0 pounds 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 ononaphthalene sulfonic acid sold by the Diamond Shamrock Process Chemicals, Inc. of Morristown, New 0 Jersey) were charged in a Kennedy Van Saun 3 ft diameter x 5 ft 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 5 diameter, 43 weight % of balls of 1.5 inch diameter, 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 0 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. 5 In substantial accordance with the procedure of EXAMPLE 2, the particle size distribution of the slurry produced in the ball mill were determined by sieve analysis and by Sedigraph 5500L analysis. The sieve analysis indicated the amount of coal particles in the 10 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 which ranged from about 74 microns to the sm-allest 15 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 20 assumption that 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 4 had a porosity of 8.096 volume percent and a specific surface area of 251.015 m 2 /cc3. This slurry produced a yield stress of about 1.0 - 2.0 Pascals at 70 volume percent solids and •' was unstable. The slurry had a Haake viscosity of 2500 cps at 100 sec" ' '. Portions of unstable slurry produced in substantial 0 accordance with EXAMPLE 4 were diluted to concentrations of either 40 weight 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 5 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 44 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 RPM. The grinding media were 2 ran diameter steel balls. The product produced by the grinding at 40% solids in the Draiswerke stirred ball mill had a D s of 6.4pm and a median size of 21.6 jjm. The surface area was 5.582 2/cm3 and the porosity 19.44 percent. The product produced by grinding at 50% solids in the Draiswerke stirred ball mill had a DL of 9-3 pm and a median size of 2.561 m; the surface area was 3.962 m? cm3, and the porosity 16.85 percent. The product by grinding at 60% solids in the Draiswerke stirred ball mill had a D 5 of 19.6 um and a median size of 4.766 m; the surface area was 2.639 m 2 /cm3 f and the porosity 12.69 volume percent. The procedure of EXAMPLE 4 was repeated, with the exception that a different charge was put in an Abbe ball mill instead of a Kennedy Van Saun ball mill. 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 4, but the surfactant concentration in the mixture was still ' 1.1 weight percent (no surfactant or caustic was added when the fine portions were ground). The properties of the surries obtained are indicated below in Table 2. 45 Table 2 if weight % type Volume Porosity Surf. BIngham Zeta slurry fines percent % area viscos. pot. added to added solids m 2 /cm3 °P mV Abbe mill 0 64 7. . 3 σ, .96 13D0 -43. .36 5Λ «J0 6-4 6. ,Q0 1, .16 1500 -42. .67 10A HΌ% 61 10. .97 1, .2 1250 -12. ,29 5 0* 64 6. ,21 1, .80 1850 -41. ,59 5B 50% 61 7. ,47 1. .08 1800 -38.57 10B 50% 64 6. .43 1, .38 1150 -10. .53 15B 50% 64 • 6. ,68 1, .38 1700 -10.78 5C 60* 64 9. 30 0, .97 1350 -33. .94 10C 60 61 6. .30 1, .02 1850 -11. .13 15C 60% 64 4. .99 1. .18 1200 -41. .52 Example 5 - Preparation of coal/water slurry 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 RPM for about 20 hours. The ground coal produced in this ball mill was 99-5% < 11.9 m, with a median size of 8.23 pm. The surface area was 1.48 rn^/ u , and porosity was 12.31 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 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 LomarB . This mixture was ground until the mixture contained at least about 98.5 percent of the 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 of about 1030 centipoise at 71 weight percent solids at 100 sec -" *. Particle size analysis of the coal consist of the slurry indicated that the consist had a porosity of 5.11 percent, and a specific surface area of 0.94 m? cm3. 10 Example 6 - Preparation of coal/oil slurry Low-volatile Upper Freeport coal from Bayard, West Virginia was used to prepare a coal-water slurry comprised of 75.2 weight percent solids which had a Haake viscosity (measured on the Haake viscometer) of 1000 centipoise at 15100 sec"^. This slurry was mixed with a volume of ethanol equal to about 60 percent of its volume and then allowed to dry for four days at about 60° centigrade at the end of which time its solids content was measured and found to be about 93 * 9% by weight. To 276.8 grams of this coal 20was added 131.0 grams of #2 fuel oil. This gave a slurry of about 63.7% by weight. The specific gravity of the oil was found to be about 0.8298 grams by a pycnometer method at ambient conditions. Therefore the slurry was about 52.2% coal by volume. 25 This slurry was measured on the Haake viscometer. It was found to be continuously shear thinning (or pseudoplastic) up to 500 sec" 1 and above. The minimum viscosity under varying viscometer conditions varied between about 250 cps and about 60 cps at 70°F. 30 Coal water slurries of this type usually double in viscosity, with about every 2.5 wgt % increase in solids. If that rule may be applied here, using 250 cps at 63.7% by weight coal, the slurry would be about 2000 cps at 71.2% coal by weight. Using 60 cps as a starting point, 35 the slurry would be 76.2% coal by weight at 2000 cps. 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 scope and spirit of the invention as defined in the following claims. SHEET

Claims: I claim: 1. A grinding mixture with a pH of from about 5 to about 12, which mixture is comprised of from about 60 to about 82 volume percent of solid carbonaceous material, from about 18 to about 40 volume percent of liquid, and from about 0.01 to about 4.0 weight percent, by weight of dry solid carbonaceous material, of dispersing agent, wherein: (a) said grinding mixture is comprised of at least 10 one fine consist of solid carbonaceous material and at least one coarse consist of solid carbonaceous material, and (b) at least about 5 weight percent of the solid carbonaceous material in said grinding mixture 15 is comprised of solid carbonaceous particles which are substantially all smaller than about 53 microns. 2. The grinding mixture as recited in claim 1, wherein . said solid carbonaceous material is selected from the 20 group consisting of coal, coke, and mixtures thereof. 3. The grinding mixture as recited in claim 1, wherein said solid carbonaceous material is coke. 4. The grinding mixture as recited in claim 1, wherein said solid carbonaceous material is coal. 255. The grinding mixture as recited in claim 1, wherein the pH of said grinding mixture is from about 7 to about 11, and from about 5 to about 20 weight percent of the solid carbonaceous particles in the grinding mixture are smaller than 53 microns. 306. The grinding mixture as recited in claim 5, wherein said grinding mixture is comprised of at least about 70 volume percent of said solid carbonaceous material. 7. A process for preparing a solid-liquid slurry, comprising the steps of: 35 (a) providing the grinding mixture of claim 1; and (b) grinding said mixture until a solid-liquid -slurry is produced wherein: C 49 1. the consist of solid carbonaceous solid material in said slurry contains at least about 5 weight percent of colloidal carbonaceous particles which are smaller than 3 microns and the net zeta potential of said colloidal carbonaceous particles is from about 15 to about 85 millivolts; 2. the solid carbonaceous particles in said slurry consist have a particle size c.£?ι " ■ BSTITUTE SH E ET 3 50 distribution substantially in accordance with the following CPFT formula: k where L XΛ = 1.0 J=ι J and where if D < D ε J » 0.0 and where if D > DL., * 1.0 wherein: 1. CPFT is the cumulative percent of said coke material finer than a certain specified particle size D, in volume percent; 2. k is the nunber of component distributions 10 in the compact, and is at least 1; 3. Xj is the fractional amount of the component j in the compact, Is less than or equal to 1.0, and the sun of all of the Xj's in the compact is 1.0; 15 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. compact and ranges from about 0.05 to about 1180 microns; 20 6. D s is the diameter of the smallest particle in fraction j, measured at 1% CPFT on a plot of CPFT versus size I), is less than L, and is greater than 0.05 microns; 7. DL is the dismieter of the largest particle in fraction j, measured by sieve size or its equivalent, and is from about 15 to about 1180 microns; and 8. no more than about 0.05 volume percent of the coke particles in the compact have a diameter less than about 0.05 microns. 3« the concentration of carbonaceous material in said slurry, the specific surface area of said consist, and the zeta potential of said colloidal particles are interrelated in _OHP ϋ- E SHEET accordance with the following H formula: v ' β ε + D + SA + 240 ZP H wherein: 1. V s is the percent, by volume, of coke material in said slurry; . 2. P is the porosity of said consist in the slurry, in percent; 3. S.A. is the specific surface area of said consist in said slurry, in square meters per cubic centimeter; 4. Z.P. is the net zeta potential of said colloidal size particles of carbonaceous material in said consist, in millivolts, and 5. H is from about 75 to about 98, 4. said slurry is comprised of at least about 60 volume percent of solid carbonaceous solid material, less than about 40 volume percent of said liquid, and from about 0.01 to about 4.0 weight percent (based upon the weight of dry coke) of dispersing agent; 5. said slurry has a yield stress of from about 3 to about 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; and 6. said.slurry is comprised of a consist which has a specific surface area of from about 0.8 to about 4.0 square meters per cubic centimeter and an interstitial porosity of less than 20 volume percent. 8. The process as recited in claim 7, wherein said solid carbonaceous material is selected from the group consisting of coal, coke, and mixtures thereof, 9. The process as recited in claim 7, wherein said solid carbonaceous material is coke. 5 10. The process as recited in claim 7, wherein said solid carbonaceous material is coal. 11. A coke compact comprising finely divided coke particles, characterized in that said coke compact comprises finely divided coke particles having a particle size 1 in the range of 1180 microns to 0.05 microns, with from about 5 to about 70 volume percent of the coke particles being smaller than about 3 microns, wherein said coke particles in said compact have a particle size distribution substantially in accordance with 15 the CPFT formula described in claim 7. 12. The^compact as recited in claim 11, wherein from about 5 to about 30 weight percent of the coke particles in said compact are smaller than about 3 microns. 13. The compact as recited in claim 11, wherein: 20 ( a ) said k is from about 1 to about 30, (b) said n is from about 0.001 to about 10, and (c) DL is from about 30 to about 420 microns. 14. The compact as recited in claim 13, wherein n is from about 0.01 to about 1.0, and k is 1.. 2515. The compact as recited in claim 14, whrein n is from about 0.01 to about 0.5. • 16. T e compact as recited in claim 15, wherein D s is from about 0.05 to about 0.20. 17. A coke-liquid slurry, comprised of at least 60 volume 30 percent of the compact of claim 11, wherein, in said slurry: (a) the consist of coke material in said slurry contains at least about 5 weight percent of colloidal coke particles which are smaller 5 than 3 microns; (b) the coke particles in said slurry consist have a particle size " ϊ- OM UBSTITUTE SHEET i Wi ' distribution substantially in accordance with the CPFT formula described in claim 7. (c) said slurry is comprised of at least about 60 volume percent of solid carbonaceous 5 solid material, less than about 40 volume percent of said liquid, and from about 0.01 to about 4.0 weight percent (based upon the weight of dry coke) of dispersing agent; (d) said slurry has a yield stress of from about 10 3 to about 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; 15 (e) said consist has a specific surface area of from about 0.8 to about 4.0 square meters per cubic centimeter and an interstitial porosity of less than 20 volume percent; (f) the net zeta potential of said colloidal 20 particles of coke material is from about 15 to about 85 millivolts. 18. The slurry as recited in claim 17, wherein said liquid is oil. 19. The slurry as recited in claim 17, wherein said 25 liquid is a mixture of water and oil. 20. The slurry as recited in claim 17, wherein k is from about 1 to about 30, n is from about 0.001 to about 10, and DL is from about 30 to about 420 microns. 21. The slurry as recited in claim 20, wherein: 30 (a) said k is from about 1 to about 30, (b) said n is from about 0.001 to about 10, and (c) DL is from about 30 to about 420 microns. 22. The slurry as recited in claim 21, wherein n is from about 0.01 to about 0.5. 3523. The slurry as recited in claim 22, wherein D 5 is from about 0.05 to about 0.20. 24. A process for preparing a coke-liquid slurry, comprising the steps of mixing from about 60 to about 82 parts by volume of the compact of claim 11 with from about 18 to about 40 parts by volume of liquid and from about 0.1 to about 4.0 parts by weight of dispersing agent 5 (by weight of dry coke in the compact). 25. The process as recited in claim 24, wherein said liquid is water * 26. The process as recited in claim 24, wherein said liquid is oil. 1027. The process as recited in claim 24, wherein said liquid is a mixture of water and oil. 28. The process as recited in claim 24, wherein k is from about 1 to about 30, n is from about 0.001 to about 10, and DL is from about 30 to about 420 microns 1529. The process as recited in claim 28, wherein n is from about 0.01 to about 1.0, and k is 1. 30. The process as recited in claim 29, wherein n is from about 0.01 to about 0.5. 31. The process as recited in claim 30, wherein D s is from 0 about 0.05 to about 0.20. 32. A solid-liquid slurry comprised of from about 60 to about 82 volume percent of solid carbonaceous material, from about 18 to about 40 volume percent of liquid, and from about 0.01 to about 4.0 weight percent 5 (by weight of dry carbonaceous material) of dispersing agent, wherein said slurry contains a carbonaceous consist comprising finely divided carbonaceous particles having a particle size distribution substantially in accordance with the CPFT formula described in claim 7 0 and whose properties are in substantial accordance with the properties of the slurry described in claim 16, and wherein the liquid in said slurry comprises a mixture of water and oil. 33- The slurry as recited in claim 32, wherein said solid 5 carbonaceous material is coal. 34. The slurry as recited in claim 32, wherein said solid carbonaceous material is coke. O SHEET s - y, V JL

Inventors: FUNK JAMES E, FUNK, JAMES, E.
Applicants: UNIV ALFRED RES, ALFRED UNIVERSITY RESEARCH FOUNDATION, INC.
Application year: 1983
Main classification: C10L1
IPC codes: C10L1