COAL-WATER FUEL SLURRIES AND PROCESS FOR MAKING

Abstract: Coal-water fuel slurries having long-term storage stability and improved viscosities and comprising finely-divided coal having a particle size distribution which is 100% -50 mesh (-297µ) and at least 50% -200 mesh (-74µ) said coal being in an amount sufficient to provide a suitable coal concentration in the slurry so as to remain within efficient combustion size range, water, and minor amounts of alkali metal salts of organic disper­ sants to reduce the viscosity of the slurry and alkaline earth metal salts of organic dispersants to obtain a higher slurry yield point and provide a substantially stable static dispersion and a process for making such slurries.

Description: Coal-Water Fuel Slurries and a process for making same. This invention relates to a high fuel value coal-water slurry which can be injected directly into a furnace as a combustible fuel can supplant large quantities of expensive fuel oil presently being used by utilities, factories, ships, and other commercial enterprises. For many years, coal-water slurries have been successfully transported long distances by pipeline to point of use, such as a utility. Since practical, cost-effective pipeline slurries do not possess the requisite characteristics for efficient use as fuels, present practice is to dewater, grind the dried coal cake to finer particle sizes, and spray the dried solid particles into the combustion chamber. Pipeline and fuel coal-water slurries differ markedly in required characteristics because of their different modes of use. For efficient, low-cost service, slurries which are pumped through pipelines for long distances should have the lowest possible viscosities and rheology which is preferably Newtonian with zero or negligible yield point. In practice, these requirements are achieved by coal concentrations which are considerably smaller than those desired in the fuel slurry. Particle sizes in the upper end of the size distribution range are excessively large for efficient combustion. A typical long-distance pipeline slurry containing no dispersant has a coal concentration of about 40 to 50% and a particle size distribution of 8M x O (U. S. Standard Sieve) with about 20% being - 32 5M ( 44(A). A great deal of work has been done to make possible higher loadings in pipelinable slurries by adding a suitable organic dispersant which reduces viscosity and improves particle dispersion. A dispersant which has been of particular interest is an anionic compound in which the anion is a high molecular weight organic moiety and the cation is monovalent, e. g., an alkali metal, such as Na or K. The anion attaches to the coal particles to give them a high negative charge or zeta potential, which causes repulsion sufficient to overcome Van der Waal's attraction and, thereby, prevent flocculation with concomitant reduction in viscosity. In accordance with DLVO theory, small monovalent cations maximize the desired negative zeta potential. This phenomenon is discussed in Funk U. S. 4, 282, 006, which also advises against the use of multivalent cations because they act as counterions which disadvantageously reduce zeta potential. The monovalent salt dispersants have been found to give essentially zero yield points. Pipeline slurries, including those containing the anionic alkali metal organic dispersants, when at rest, tend to separate gravitationally in a short period of time into supernatant and packed sediment which is virtually impossible to redisperse. For efficient practical use as a fuel, the slurry must have several essential characteristics. It must have long-term static stability so that it can be stored for extended periods of time by suppliers or at the point of use. During such storage, they must remain uniformly dispersed or, at most, be subject to some soft subsidence which can be easily redispersed by stirring. By subsidence is meant a condition in which the particles do not segregate, as in sedimentation, but remain dispersed in the carrier fluid in a gel or gel-like formation. Uniform dispersion is essential for reliably constant heat output. Coal loadings must be sufficiently high, e. g., up to 65 to 70% or higher, to produce adequate fuel value despite the presence of the inert water carrier. The coal particles must be small enough for complete combustion in the combustion chamber. The slurry must also be sufficiently fluid to be pumped to and sprayed into a combustion chamber. However, the low viscosities required for pipelinable slurries are not required for a fuel slurry. Such fuel slurries have eluded the commercial art. It is obvious that a process which can convert coal directly into a fuel slurry or transform pipeline slurry at its terminal into a fuel slurry having the aforedescribed characteristics without requiring dewatering of the coal to dryness would be most advantageous. Coal-water slurries which have the requisite properties for effective use as fuels are disclosed in copending European patent application nos. 81304187. 8 and 83301195. 0. These applications teach the use of alkaline earth metal organosulfonate dispersants to form stable coal-water fuel slurries which have a coal-loading capacity as high as 70% or more and particular bimodal particle size distributions. The divalent metal salt acts both as dispersant and slurry stabilizer. The fuel slurries are thixotropic or Bingham fluids which have yield points; become fluid and pourable under relatively small stresses to overcome the yield point; and have the long-term static stability required for a practical fuel. The viscosities of these slurries, though not excessively large for handling and use, are considerably higher than those obtained with the alkali metal salts. Generally, the prior art has focused on reducing viscosity and, thereby, increasing loadings and pumpability of pipeline slurries. The art has taught the use of anionic alkali metal and alkaline earth metal organic dispersants as equivalents for these objectives, and have shown the alkali metal dispersants to be superior. None of the references teach or suggest the unique capability of the alkaline earth metal salts as long-term static stabilizers or their combination with alkali metal salt derivatives to produce the stable fuel slurries of the present invention. References of interest include Wiese et al. 4, 304, 572 and Cole et al. 4, 104, 035 which disclose the use of alkali metal and alkaline earth metal salts of organosulfonic acids to improve slurry loading and pumpability. In both cases the data show the alkali metal salts to be superior for the stated objectives. An object of the present invention is to provide a coal-water fuel slurry and a method of making such a slurry. According to the present invention there is provided a coalwater fuel slurry which comprises: a. admixing i. finelydivided coal having a particle size distribution which is 100% -50 mesh(-297li)and at least 50% -200 mesh (-74r) said coal being in amount sufficient to provide a desired coal concentration in the slurry; ii. a minor amount of anionic monovalent cation salt organic dispersant sufficient to reduce substantially the viscosity of the slurry; iii. a minor amount of anionic alkaline earth metal salt organic dispersant sufficient to produce a slurry yield point larger than that obtained with said monovalent cation salt alone and to maintain the slurry in substantially stable static dispersion; ; iv. water, and b. subjecting the mixture to high shear mixing at a shear rate -1 of at least 100 sec Still further according to the present invention there is provided a process for converting a coal-water pipeline slurry into a substantially stable fuel slurry, wherein the pipeline slurry contains particles of excessive size for efficient combustion, which comprises: : a. partially dewatering or adding finely-divided coal in an amount sufficient to increase the coal content in the pipeline slurry to a concentration desired in the fuel slurry, if the coal concentration in the aqueous pipeline slurry is less than that desired in the fuel slurry; b. passing said slurry through a comminuting means to reduce excessively sized coal particles to sizes sufficiently small for combustion in a combustion chamber and to produce a particle size distribution of 100% -50 mesh (-297P) and at least 50% -200 mesh (-74P). c. adding to the slurry a minor amount of: (i) an anionic monovalent cation salt organic dispersant sufficient to reduce substantially the viscosity of the slurry, and (ii) an alkaline earth metal salt organic dispersant sufficient to produce a slurry yield point larger than that produced with said monovalent cation dispersant alone and to maintain the slurry in a substantially stable static dispersion; and d. subjecting the mixture comprising said coal, said monovalent cation and alkaline earth metal dispersants and water to high shear mixing at a shear rate of at -1 least about 100 sec The coal particle sizes should be within a range small enough for efficient combustion; 100% of the coal should be -50M (-297,u and at least 50% -200M (-74,). Preferably, at least about 65% is -200M 74 > ). A particularly suitable coal size distribution is prepared from a bimodal mixture comprising about 10 to 50% wt. %, preferably 10 to 30 wt. % on slurry, of particles having a size up to about 30 MMD (mass median diameter), preferably about 1 to 15/ MMD, as measured by a forward scattering optical counter, with the rest of the coal particles having a size range of about 20 to 200/t MMD, preferably about 20 to 150z44 MMD. Crushed coal can be ground in known manner to produce the particle sizes required for preparation of the fuel slurries. The actual degree of coal loading is not critical so long as it is sufficient to provide adequate heat output. The maximum concentration of coal successfully incorporated into a given slurry may vary with such factors as particle size distribution, the particular dispersants used and their total and relative concentrations. The alkali metal salt organic dispersant is added to the slurry in an amount sufficient to impart substantially reduced viscosity. As will be seen from the Examples below, the slurries containing only the alkali metal salt generally do not have a yield point. The alkaline earth metal salt organic dispersant is added to the slurry in an amount sufficient to impart a substantial yield point and to maintain the slurry in stable dispersion for extended storage period without separation of the coal particles into packed sediment. Long term static stability requires either a thixotropic or Bingham fluid with an appreciable yield point. The optimum amount which will accomplish the desired results without excessive increase in yield point or viscosity can readily be determined by routine tests in which the amounts and ratios of the alkali metal and alkaline earth metal salt dispersants are varied. It is believed that the relative proportions of the available alkali metal and alkaline earth metal cations provided by the respective dispersants play an important role in imparting stability and determining yield point and viscosity. However, so many other factors, such as the particular coal, the particular particle size distribution, and the particular dispersant anions, also effect rheological properties in varying and generally unquantifiable degree, that it is difficult to specify generically an optimum ratio of the mono- and divalent cations which would necessarily apply to different specific slurries. In general, however, a ratio in mmols/100 g coal of the monovalent to divalent cations, e. g. Na+:Ca++, equal to or smaller than 2:1, produces stable soft gels, with increase in yield point and viscosity as the proportion of multivalent ions increases. The anionic alkali metal (e. g., Na, K) and anionic alkaline earth metal (e. g., Ca, Mg) organic dispersants preferably have organic moieties which are multifunctional and high molecular weights, e. g. about 1, 000 to 25, 000. Examples of useful dispersants include organosulfonates, such as the Na lignosulfonates, Na napthalene sulfonates, Ca lignosulfonates, and Ca napthalene sulfonates, and organo carboxylates, such as Na lignocarboxylate. The alkali metal and alkaline earth metal organosulfonate are preferred. The total amount of the two types of dispersant used is minor, e. g. about 0. 1 to 5 pph coal, preferably about 0. 5 to 2 pphc. In some cases, it may be desirable to add an inorganic alkali metal (e. g., Na, K) salt or base to control pH of the slurry in the range of about pH 4 to 11. This may improve aging stability, pourability, and handling characteristics of the slurry. The salt, such as sodium or potassium phosphate, including their acid salts, or the base, such as NaOH or KOH, is used in minor amounts sufficient to provide the desired pH, e. g., about 0. 1 to 2% based on the water. The inorganic salts also serve to reduce gaseous sulfur pollutants by forming non-gaseous sulfur compounds. Other additives which may be included are biocides and anti-corrosion agents. The finely-divided coal particles, water1 and dispersants are mixed in a blender or other mixing device which can deliver high shear rates. High shear mixing, e. g., at shear rates of at least about 100 sec-l preferably at least about 500 sec 1, is essential for producing a stable slurry free from substantial sedimentation. The slurries can generally be characterised as either thixotropic or Bingham fluids having a yield point. When at rest, the slurries may gel or flocculate into nonpourable compositions which are easily rendered fluid by stirring or other application of relatively low shear stress sufficient to overcome the yield point. They can be stored for long periods of time without separation into packed sediment. They may exhibit some soft subsidence which is easily dispersed by stirring. Slurries embodying these characteristics are included in the term '1stable, static dispersions" as employed in the specification and claims. The slurries can be employed as fuels by injection directly into a furnace previously brought up to ignition temperature of the slurry. In addition to preparing the stable fuel slurry directly from dry coal ground to the desired particle sizes as aforedescribed, the invention can be employed to convert a pipeline slurry at its destination into a fuel slurry and, thereby, eliminate the present costly requirement for complete dewatering. The process of the invention is highly versatile and can be applied to a wide variety of pipeline slurries. The details of the conversion process are determined by the make-up of the particular pipeline slurry, As aforedescribed, pipeline slurries generally have lower coal concentrations and larger particle sizes than are required for effective fuel use and may or may not include a viscosity-reducing alkali metal salt organic dispersant. In the case of pipeline slurries which do not contain dispersant, the following procedures can be used. Coal concentration can be increased to fuel use requirements by partial dewatering or by addition of coal. After such adjustment the slurry is passed through a comminuting device, such as a ball mill, to reduce the coal particles to the desired fuel size. It should be noted that increasing concentration by coal addition can be done after ball milling, but preferably precedes it. Addition of the alkali metal and alkaline earth metal organi dispersants can be done after the milling. Preferably at least some to all of the alkali metal or alkaline earth metal dispersant or some to all of both are added to the coal-water slurry prior to milling. When only a portion of the dispersant(s) is added during milling, the remainder is added subsequently, together with any other additives such as biocides, buffer salts1 bases and the like. The slurry mixture is then subjected to high shear mixing, as aforedescribed. The amount and ratio of total alkali metal and alkaline earth metal dispersants added for optimum stability viscosity and yield point are determined by routine tests as aforedescribed. In the case of pipeline slurries which include an alkali metal organic dispersant to reduce viscosity and increase coal concentration, the following procedures can be used: If the coal concentration is inadequate for fuel use, it can be adjusted by partial dewatering or addition of coal. If coal concentration in the pipeline slurry is adequate, this step can be omitted. Generally, coal particle sizes are larger than desired for fuel use for reasons of reducing viscosity, so that the slurry requires passage through a milling device. The slurry contains its original alkali metal organic dispersant which assists in the milling procedure. Some or all of the alkaline earth metal dispersant can also be added to the wet milling process. After determination of the concentration of alkali metal salt dispersant in the pipeline slurry, the optimum amount of alkaline earth metal dispersant and any additional alkali metal dispersant required is determined by routine test. After addition of dispersant and any other desired additives1 such as biocides, buffer compounds, bases and anti-corrosion agents, the slurry mixture is subjected to high shear mixing. The fuel slurries made from the long distance pipeline slurries are substantially the same as those produced directly from dry coal. Fuel slurries, as prepared in accordance with the present invention, have substantially lower viscosities than those obtained with the divalent salts alone, while retaining the same long-term static stability and other properties required for use as a fuel, and therefore important advantages in terms of ease of handling and power consumption. DETAILED DESCRIPTION Example 1 A series of slurries containing 65% by weight of Kentucky bituminous coal was prepared with 1. 0 pph coal, (0. 65% slurry) of a mixture of Na and Ca lignosulfonates and with 0. 5 and 1. 0 pphc of the Na or Ca dispersant only. The coal was a bimodal blend comprising 70% of a coarse fraction having an MMD of 110 and a maximum size of about 300ir and 30% of a fine fraction having an MMD ranging from about 5 to 10r (45. 5 and 19. 5% respectively by weight of slurry). The size consist of the blend was 58% -200M. The larger particle sizes were determined by sieving. Sub-sieve particle sizes were determined by a forward scattering optical counter which is based on Fraunhofer plane diffraction. The coarse fraction was prepared by hammermilling and sieving through a 50 mesh (297r) screen. The fine grind was prepared by wet ball milling for 2 hours. Except for run MR-16 which was made without any dispersant, all of the wet ball milling was done with at least a portion of dispersant. All of the ball mill runs were made with a 50% coal mill the remainder being dispersant and water. Runs N11-l, MR-1-4, and MR-6-8 were milled with Na dispersant; runs 9-11, with a portion of both Na and Ca dispersant, and runs 12 and 13 with a portion of the Ca dispersant. Preferably, though not essentially, the coal is milled with water so that the very fine particles are in water slurry when introduced into the mixer. At least some of the dispersant is included in the ball milling operation to improve flow and dispersion characteristics of the fine particle slurry. The fuel slurry blends were prepared by mixing the coarse fraction, the fine ball-milled fraction, additional dispersant, and water in the amounts required for the desired slurry composition. The amounts of the Na and Ca dispersants were changed to vary the ratio of the Na and Ca cations. The weight ratio of Na to Ca dispersant was varied from 1:0 to 0:1 pphc at increments of 0. 1 pphc. The consequent Na:Ca molar ratio was varied from 3. 9:0 to 0:2.2 mmols/l00g coal. The particular dispersants used were Marasperse CBOs-3, a sodium lignosulfonate containing 3. 91% Na and 0. 075% Ca by weight1 and Norlig lld, a calcium lignosulfonate containing 2. 175% Ca. The compositions were mixed in a high-shear blender at -l 6000 rpm at a shear rate of about 1000 sec Results are summarized in Table 1. With no dispersant, MR-16 has a yield point of 723 dynes/cm2 -l and a viscosity of 32, 500 p at a shear rate of 10 sec , which make it unusable as a pipeline or fuel slurry. Additon of 0. 5 or 1 pphc (comps MR-8 and Nll-1 respectively) of the Na dispersant reduces yield point to zero and viscosities to the desirable low values of 5. 6 and 4. 9 p respectively. Rheology is essentially newtonian. The slurries, however, have no appreciable static stability, which makes them unfit for use as a fuel. As shown by slurries MR-12 and 13, addition of the Ca dispersant alone at 1. 0 and 0. 5 pphc, also reduces viscosity to 9. 96 and 11. 5 p respectively, but to a substantially lesser degree than the Na dispersant alone. Unlike the Na dispersant slurries, the Ca salt slurries have substantial yield points, 2 12. 8 and 11. 4 dynes/cm respectively, and long-term stability without hard packed sediment. Thus, the Ca dispersant is functioning both as dispersant and stabilizer. It can be further seen from the experimental data in Table 1 that when the Na and Ca dispersants are both used in the slurries in relative amounts which vary incrementally and which thereby vary the Na:Ca ion ratios, and the Ca dispersant concentration is sufficient to produce a yield point, both viscosity and yield point are substantially reduced as compared with Ca dispersant alone without sacrificing the long-term static stability essential for a storable fuel slurry. For example MR-6, a very stable slurry, contains 0. 5 pphc of the Na dispersant and 0. 5 pphc of the Ca dispersant. TABLE 1 EMI13.1 Dispersant <SEP> Ion <SEP> Content, <SEP> Rheological <SEP> Constants <tb> Content, <SEP> pphc <SEP> mmols <SEP> per <SEP> Na:Ca <SEP> Yield <SEP> Viscosity, <tb> Composition <SEP> Marasperse <SEP> Norlig <SEP> 100 <SEP> g <SEP> Coal <SEP> Molar <SEP> Point <SEP> Poise, <SEP> @ <SEP> Stability <SEP> Notes <tb> ID <SEP> CBOs-3 <SEP> lld <SEP> Na <SEP> Ca <SEP> Ratio <SEP> dynes/cm2 <SEP> 10 <SEP> sec-1 <SEP> Days <SEP> Observations <tb> MR-16 <SEP> 0 <SEP> 0 <SEP> 0 <SEP> 0 <SEP> - <SEP> 723 <SEP> 32,500 <SEP> 8 <SEP> Thick <SEP> dough <tb> MR-8 <SEP> 0.5 <SEP> 0 <SEP> 2.0 <SEP> 0.038 <SEP> 53 <SEP> 0 <SEP> 5.6 <SEP> 1 <SEP> Unstable <SEP> * <tb> N11-1 <SEP> 1.0 <SEP> 0 <SEP> 3.9 <SEP> 0.075 <SEP> 52 <SEP> 0 <SEP> 4.9 <SEP> 1 <SEP> Unstable <SEP> * <tb> MR-1 <SEP> 0.9 <SEP> 0.1 <SEP> 3.5 <SEP> 0.22 <SEP> 16 <SEP> 0 <SEP> 2.9 <SEP> 1 <SEP> Unstable <SEP> * <tb> MR-2 <SEP> 0.8 <SEP> 0.2 <SEP> 3.1 <SEP> 0.44 <SEP> 7.0 <SEP> 0 <SEP> 3.1 <SEP> 1 <SEP> Unstable <SEP> * <tb> MR-3 <SEP> 0.7 <SEP> 0.3 <SEP> 2.7 <SEP> 0.65 <SEP> 4.2 <SEP> 0 <SEP> 2.2 <SEP> 1 <SEP> Unstable <SEP> * <tb> MR-4 <SEP> 0.6 <SEP> 0.4 <SEP> 2.3 <SEP> 0.87 <SEP> 2.6 <SEP> 1.0 <SEP> 3.7 <SEP> 12 <SEP> Stable <SEP> ** <tb> MR-6 <SEP> 0.5 <SEP> 0.5 <SEP> 2.0 <SEP> 1.1 <SEP> 1.8 <SEP> 3.8 <SEP> 5.1 <SEP> 12 <SEP> Stable <SEP> ** <tb> MR-7 <SEP> 0.4 <SEP> 0.6 <SEP> 1.6 <SEP> 1.3 <SEP> 1.2 <SEP> 6.9 <SEP> 6.3 <SEP> 12 <SEP> Stable <SEP> ** <tb> MR-9 <SEP> 0.3 <SEP> 0.7 <SEP> 1.2 <SEP> 1.5 <SEP> 0.8 <SEP> 14.2 <SEP> 9.5 <SEP> 11 <SEP> Stable <SEP> ** <tb> MR-10 <SEP> 0.2 <SEP> 0.8 <SEP> 0.78 <SEP> 1.7 <SEP> 0.5 <SEP> 13.5 <SEP> 11.2 <SEP> 11 <SEP> Stable <SEP> ** <tb> MR-11 <SEP> 0.1 <SEP> 0.9 <SEP> 0.39 <SEP> 2.0 <SEP> 0.2 <SEP> 7.8 <SEP> 11.3 <SEP> 11 <SEP> Stable <SEP> ** <tb> MR-12 <SEP> 0 <SEP> 1.0 <SEP> 0 <SEP> 2.2 <SEP> 0 <SEP> 12.8 <SEP> 10.0 <SEP> 10 <SEP> Stable <SEP> ** <tb> MR-13 <SEP> 0 <SEP> 0.5 <SEP> 0 <SEP> 1.1 <SEP> 0 <SEP> 11.4 <SEP> 11.5 <SEP> 10 <SEP> Stable <SEP> ** <tb> * Separated into supernatant with hard packed sediment. ** Soft non-pourable thixotropic gel with small supernatant and no packed sediment. Comp MR-4 showed some soft sediment. All mixes became fluid and pourable with easy stirring. Its yield point is 3.8 dynes/cm2 as compared with zero for the MR-8 which contains only 0. 5 pphc of Na dispersant and 11. 4 2 dynes/cm for the MR-13 which contains only 0. 5 pphc Ca dispersant. the Viscosity of Comp MR-6 at a shear rate of -1 10 sec is 5.1 p as compared with 5.6 p for MR-8 and 11.5 p for MR- 13. In MR-4 relative reduction in yield point and viscosity, with an Na and Ca dispersant pphc ratio of 0. 6 to 0. 4, is even greater. Stability of this slurry is good, though somewhat less than that of MR-6. It is interesting to note that an optimum combination of low yield point, low viscosity, and excellent stability is achieved at a Na:Ca ratio of about 2:1 and that excellent stability is maintained with smaller incremental ratios but with increasing viscosities as the proportions of Ca ion increase. The slurries are still stable after 10 to 12 days in storage. These tests demonstrate the unique properties of the anionic alkaline earth metal salts of an organic dispersant as both dispersants and fuel slurry stabilizers and the improvement in viscosity and reduced yield points obtained when they are combined with anionic alkali metal salts of organic dispersants. Example 2 A monomodal coal particle size distribution was prepared by dry ball milling crushed "FPL" bituminous coal to a size consist such that 100% was -50M (297ft) and 70% was -200M 74). This coal consist is frequently called "boiler grind" and is comparable to the state-of-the-art practice for dry directfiring coal-fired furnaces. Slurries of 65% coal in water were prepared by admixing the comminuted coal with water, Marasperse CBO-3 (Na salt) and Norlig 11d (Ca salt) in selected ratios. All of the mixes were subjected to high shear mixing. The results are summarized in Table 2. Table 2 PARAMETER COMP ID FPL 34 MR-8AA FPL 33 A. Dispersant Content, pphc Marasperse CBOs-3 0.25 0.50 1.0 Norlig ild 0.50 0.50 0.50 B. Ion Content, mmols/100 g coal Na 0.98 2.0 3.9 Ca 1.1 1.1 1.2 C. Na:Ca Molar Ratio 0.88 1.8 3.3 D. Rheologicals Yield point, dynes/cm2 12.8 0.5 0 Viscosity at a shear rate of 10 sec-1, p 8.9 3.3 2.9 E. Stability &commat; 24 hours Supernatant liquid Slight No Yes Subsidence bed Non-pourable gel Pourable Hard packed Sedimentation No Very soft, pourable Stability at one week Soft, non-pourable Supernatant and soft, gel; No sediment restirrable sediment Stability at two weeks Medium non-pourable Supernatant packed gel; No sediment subsidence bed These results clearly show that as the Na;Ca ratio is decreased from 3. 4:1, yield point, viscosity and stability are increased. The slurry is stable at 0. 88:1, marginal at 1. 8:1 and unstable at 3. 4:1. It is evident that viscosity and yield point increase significantly with decreasing Na:Ca ratio. Thus, at Na:Ca ratios between 1. 8 and 0. 88, stable fuel slurries can be obtained at lower viscosities than could be obtained with the Ca dispersant stabilizer alone. Example 3 A 65 wt. % pipelinable FPL bituminous coal-water slurry was prepared by mixing 39 parts of a coarse fraction crushed to lOM (2000 ) x 0 with an MMD of 350 ; 26 parts of a fine coal fraction wet ball milled to 325M (441l) x 0 and an MMD of 7. 8 ; 0. 447 parts of marasperse N22, a sodium lignosulfonate containing 2. 91 mmol Na and 0. 15 mmol Ca per 100 g coal, and a total of 34. 228 parts water. The coal, water and Na dispersant were mixed in a Hobart mixer. Viscosity of the mix was 1. 5 p at 50 rpm Brookfield. Although the slurry was exceedingly unstable at rest, the very low viscosity obtained with the Na lignosulfonate dispersant makes it useful as a long-distance pipeline slurry. To the above slurry, 0. 325 parts Norlig lld, a calcium lignosulfonate, were added. The slurry was then charged to an 8 5/8 inch diameter ball mill and milled for 15 minutes. The resulting slurry was fluid and had a size consist of 99. 6% -70M with 76. 6% -200M, which is well within the desired particle size range for efficient combustion. Upon standing overnight the slurry exhibited sediment. It was then subjected to high shear mixing at about 6000 rpm in an Oster blender. Before the high shear blending, the yield point of the slurry was 0 and viscosity was 8. 15 p at 10 sec-l. After the blending 2 the yield point was 21. 7 dynes/cm . Viscosity at 10 sec¯1 was 21. 1 p and 8. 15 p at 67 sec-l. The slurry was markedly thixotropic and very stable. At rest, it was a soft non-pourable gel with slight supernatant and no sediment after seven days. It became fluid and pourable with easy stirring. This example demonstrates successful conversion of a pipeline slurry into a stable combustible fuel slurry by: (1) addition of Ca dispersant, (2) milling to the desired reduced size consist, and (3) high shear mixing. In this case the 65% pipeline coal concentration was adequate for efficient use as a fuel. It should be understood that if coal concentration in the pipelinable slurry is inadequate, it can be increased by partial dewatering or addition of dry coal. If the pipeline slurry does not contain dispersant, the alkali metal salt organic dispersant can be added prior to milling, or before or after high shear mixing, preferably before. This example also demonstrates the importance of high shear mixing in preparation of the stable fuel slurry.

Claims: Claims: 1. A coal-water fuel slurry which comprises: a. finely-divided coal having a particle size distribution which is 100% -50 mesh (-297,L() and at least 50% -200 mesh(-74 ) said coal being in amount sufficient to provide a desired coal concentration in the slurry; b. a minor amount of anionic monovalent cation salt organic dispersant sufficient to reduce substantially the viscosity of the slurry; c. a minor amount of anionic alkaline earth metal salt organic dispersant sufficient to produce a slurry yield point larger than that obtained with said monovalent cation salt alone and to maintain the slurry in substantially stable static dispersion; and d. water. 2. A slurry according to claim 1 in which the monovalent cation is an alkali metal. 3. A slurry according to claim 1 or 2 in which the finely divided coal has a particle size distribution of which at least 65% is -200 mesh (-74 > 1). 4. A slurry according to any one of claims 1 to 3 in which the alkaline earth metal salt dispersant is an organosulfonate. 5. A slurry according to claim 4 in which the alkaline earth metal dispersant is a Ca lignosulfonate.. 6. A slurry according to any one of claims 1 to 5 in which the monovalent cation salt dispersant is an organosulfonate. 7. A slurry according to claim 6 in which the monovalent cation salt dispersant is a Na or K lignosulfonate. 8. A slurry according to any one of claims 1 to 7 in which the coal particle sizes comprise: a. fine particles having a maximum size of 30 MMD (Mass Median Diameter) in an amount comprising from 10 to 50% by weight of the slurry, and b. larger coal particles within the size range of from 20 to 200r MMD, in which sub-sieve particle sizes are defined in terms of those obtainable by forward scattering optical counter. 9. A slurry according to claim 8 in which the fine particles comprise from 10 to 30% by weight thereof. 10. A slurry according to claim 8 or 9 in which the size range of the fine coal particles is from 1 to 157 < MMD and the size range of the larger coal particles is from 20 to 150zU MMD. 11. A process for making a substantially stable coal-water fuel slurry, which comprises: a. admixing: (i) finely-divided coal having a particle size distribution which is 100% -50 mesh (-29',ct) and at leasr 50% -200 mesh (-74fL ) said coal being in amount sufficient to provide a desired coal concentration in the slurry; (ii) a minor amount of anionic monovalent cation salt organic dispersant sufficient to reduce substantially the viscosity of the slurry; (iii) a minor amount of anionic alkaline earth metal salt organic dispersant sufficient to produce a slurry yield point larger than that obtained with said monovalent cation salt dispersant alone and to maintain the slurry in substantially stable static dispersion; and (iv) water, and b. subjecting the mixture to high shear mixing at a shear rate -l of at least 100 sec 12. A process according to claim 11 in which the coal particle sizes comprise: a. fine particles having a maximum size of 30/( MMD in an amount comprising from 10 to 50% by weight of the slurry; and b. larger coal particles within the size range of from 20 to 200 MMD; in which sub- sieve particle sizes are defined in terms of those obtainable by forward scattering optical counter. 13. A process according to claim 11 or 12 in which the fine particles comprise from 10 to 30% by weight of the slurry. 14. A process according to any one of claims 11 to 13 in which the size range of the fine particles is from 1 to 157 < MMD and the size range of the larger particles is from 20 to 150 MMD. 15. A process for converting a coal-water pipeline slurry into a substantially stable fuel slurry, wherein the pipeline slurry contains particles of excessive size for efficient combustion, which comprises: a. partially dewatering or adding finely-divided coal in an amount sufficient to increase the coal content in the pipeline slurry to a concentration desired in the fuel slurry, if the coal concentration in the aqueous pipeline slurry is less than that desired in the fuel slurry; b. passing said slurry through a comminuting means to reduce excessively sized coal particles to sizes sufficiently small for combustion in a combustion chamber and to produce a particle size distribution of 100% -50 mesh (-297P) and at least 50% -200 mesh (-74 ). c. adding to the slurry a minor amount of: (i) an anionic monovalent cation salt organic dispersant sufficient to reduce substantially the viscosity of the slurry and (ii) an alkaline earth metal salt organic dispersant sufficient to produce a slurry yield point larger than that produced with said monovalent cation dispersant alone and to maintain the slurry in a substantially stable static dispersion; and d. subjecting the mixture comprising said coal, said monovalent cation and alkaline earth metal dispersants and water to high shear mixing at a shear rate of at least -1 about 100 sec 16. A process according to claim 15 in which at least some of the monovalent cation dispersant is a component of the pipeline slurry. 17. A process according to any one of claims 11-16 in which the monovalent cation is an alkali metal. 18. A process according to any one of claims 11-17 in which the finely-divided coal has a particle size distribution of which at least 65% is -200 mesh (-74fl). 19. A process according to any one of claims 11-18 in which the alkaline earth metal salt is an organosulfonate. 20. A process according to claim 19 in which the alkaline earth metal salt is a Ca lignosulfonate. 21. A process according to any one of claims 11-20 in which the monovalent cation dispersant is an organosulfonate. 22. A process according to claim 21 in which the monovalent cation dispersant is a Na or K lignosulfonate.

Inventors: SCHEFFEE, ROBERT STEPHEN
Applicants: ATLANTIC RESEARCH CORPORATION
Application year: 1983
Main classification: C10L1
IPC codes: C10L1, C10L10