AU596055B2 - Coal compositions and their production - Google Patents

Description

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COMMONWEALTH OF AUSTRALIA PATENT ACT 1952 COMPLETE SPECI FICATION 596055

(ORIGINAL)

FOR OFFICE USE CLASS INT. CLASS Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Priority: Related Art-: o ~t 0 000 Ih is (j L nriwlj,,q

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NAME OF APP'LICANT: ALLIED COLLOIDS LIMITED ADDRESS OF APPLICANT: P.O. BOX 38, Low Moor, Bradford, West Yorkshire, BDl2 0J2, England.

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0 so 4 NAME(S) OF INVENTOR(S) David FARRAR Peter FLESHER Clive HAPPS Doug SHUTTLEWORTH Malcolm SKINNER ADDRESS FOR SERVICE: DAVIES COLLISON. Patent Attorneys 1 Little Collins Street, Melbourne, 3000. 0* 54 0 8 o 0 04 I 0 0 0 00 COMPLETE SPECIFICATION FOR THE INVENT~ION ENTITLED,: "COAL COMPOSITIONS AND THEIR PRODUCTION" The following statemient is a full description of this inventione including the best method Of performing it known to us:- -1- Davies Collison, Melbourne and Canberra.

1A Allied Colloids Limited 60/2654/02 Coal Compositions and their Production This invention relates to the utilisation of wet, sticky, coal fines filter cake in the production, by easy and safe techniques, of a product that can be used as, for instance, fuel for a power station, often after transportation in a truck.

Relatively large volumes of coal fines are formed during the mining of coal and during the recovery and transportation of mined coal. They have a size mainly below 0.5mmi and often considerably less. Some of the fines are separated from the coarse coal at the point of lot mining but others are washed from the coarse coal after mining. Irrespective of how they are separated, the s coal fines cause a serious problem at a coal mine (undergr und or open cast). Normally they are put into the form of a mobile slurry or a froth flotation concentrate and are then converted into a filter cake by filtration, vacuum filtration by disc or drum filters. The filtration is performed to achieve the lowest possible water content but the final filter cake, when taken off the filters and subsquently handled, is I 1 always found to be a very sticky material that is highly viscous or is semi-scalid. This very thick or semi-solid material is formed of wet coal fines and typically has a water content of around 30%. Its ash content is generally well below 30% based on solids, e og., 10 to f Its texture is such that at present it is difficult to use any or all of it and vast volumes of the filter cake are dumped.

Attempts have been made to utilise it rather than dump it. For instance the sticky mass has been blended with coal smalls prior to use as a fuel. Unfortunately 35 the fines are so sticky that they tend to clog the

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3aas 0 P B cak ar dupd Atemt hav been maet tls i ahrta tnawiurc o ucciaranil) no I t. attestation required) Note: Initial all alteralions. DAVIES COLLISON, MELBOURNE and CANBERRA.

t 2 pulverisers, conveyors and other apparatus utilised for feeding the blend to the boiler. It is therefore essential to keep the amount of fines extremely low, generally not more than 10% of the total blend, and even at these low values results tend to be unsatisfactory.

Thermal or other water removal from the sticky mass would reduce many of these problems but, since the fines include substantial amounts below 100gm, the step of drying the fines (and the use of the resultant dried fines) would be liable to increase the flash hazard of the overall process.

It is already known to convert a wet particulate mass from a non-crumbly to a crumbly state by 'incorporating certain absorbent polymeric materials into S 15 the mass, for instance as described in EP 195550. A wide variety of wet particulate materials have been described as being treated by such processes. For instance in EP 195550 there are examples of treating wet lump coal having a particle size above 1cm and of treating filter coal tailings the non-combustible tailings obtained during flotation of coal fines) having a size up to 1mm. No details are given of the mixing t methods that are used.

Most of the literature is silent about the problems S 25 of treating coal fines filter cake, despite the enormous volumes of it that have been dumped and that are produced daily. An exception is GB 2,122,218 which describes a Sprocess in which wet filter cake fines were blended with 1 coal smalls and the mixture was then blended with a S 30 binder such as cement followed by a polyelectrolyte such as the material sold under the trade name "Alcosorb".

"Alcosorb" AB1, which is what was used in that work, is substantially non-ionic and of relatively large particle size. The resultant mixture was then converted into pellets which were suitable for addition to coal blends A A L 1 ,j% i; I 3 for power station use and which tend to maintain their form up to entering the combustion chamber. It was mentioned that the process could be operated without the addition of the coal smalls or the binder, but in practice this was not done. One reason was that the coal product, if it was not pelletised, would have to go through the normal pulverisers before being burnt in power station or other boilers, and it was expected that pulverisation of a friable product containing swollen polymer would be impracticable and unsafe, due either to increased flash hazard or to clogging of the pulverisers or both. Also Alcosorb AB1 did not give adequate friability to the fines for sufficiently homogeneous mixing with coal smalls to permit use in non-pelletised form.

These problems could not have been overcome by the proposals in EP 195550. Even if those proposals had been applied to coal fines filter cake, there would still have been the problem that, when using the polymer particles proposed in EP 195550 in combination with conventional mixing methods, the improvement in friability of filter cake would have been beneficial but i insufficient for commercial scale mixing with coal smalls as a pulverisable power station feed. Also there was still serious concern that pulverisation would lead to S* increased flash hazard or to clogging of the pulverisers or both.

Accordingly the processes described in GB 2,122,218 S, and EP 195550 have not proved commercially useful for 30 coal filter cake and there is still daily production and dumping of large volumes of wet, sticky, coal fines filter cake.

In the invention non-sticky, combustible, fuel is made from sticky coal fines filter cake by a process comprising mixing particulate absorbent polymer into the I67 1 1 j|_ 3a cake, and the process is characterised in that the polymer is a non-film forming, cross linked, synthetic polymer that has a gel capacity of at least 25 grams deionised water per gram polymer and that is formed from water soluble ethylenically unsaturated monomer or monomer blend of which at least 5% by weight is ionic and the polymer is in the form of particles that are substantially non-sticky when swollen by Oft I 4t" water, and the mixing is conducted under conditions such that the cake is converted by the mixing from its sticky state to a friable form that can easily be blended substantially homogeneously with coal smalls.

Sa ta t oa t oX r.

4 polymer is a non-film forming, cross link d, synthetic polymer formed from water solu e ethylenically unsaturated monomer or monomer ble of which at least by weight is ionic and the nymer is in the form of particles that are substan tally non-sticky when swollen by water, and the mixi g is conducted under conditions such that the cak is converted by the mixing from its sticky state t a friable form that can easily be blended substantia hly with al M It is essential in the invention that the friability of the treated cake is such that it can be blended Sr, substantially homogeneously with coal smalls, i.e., :0 significant aggregates of sticky cake, generally free of smalls, are not formed. This is a convenient indication that the filter cake has a friability suitable for a variety of purposes.

Since the product of the mixing is friable, instead of being a sticky mass, problems that have been encountered previously when blending up to 10% filter cake with smalls are avoided and, indeed, it is possible to use much larger amounts of filter cake in the blend, S, up to 20% or 30% based on the weight of the blend.

SThe smalls can be any coal above lmm, generally 2 to 10mm, but they can be larger.

Although the blend can be fed into power station boilers or other industrial combustion chambers in S various physical forms, for instance in the form in which i/ r it is obtained by mixing, or after pelleting, it is 30 generally preferred for the blend to be pulverised to a particle size below 2004m, often below 100im, and for the i resulting powder to be carried in an airstream into the power station boiler or other combustion chamber. Feed to the boiler often occurs continuously with the pulverisation, but in some instances the powder may be ~~e *r

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I:li t collected in hoppers and subsequently fed to the boiler.

We have determined that the presence of swollen polymer does not cause clogging of the pulverisers.

Instead of blending the smalls after converting the cake to a friable form, some or all of the smalls can be included with the wet cake before addition of polymer.

Although the friable cake is suitable for blending with smalls, it is not essential to blend it with smalls and it can be used for a wide variety of other purposes.

It may be bonded into pellets or other shaped bodies in ways known for bonding dry powder. Generally smalls are included in order to give a range of particle sizes.

The friable cake, with or without blending with coal smalls and with or without a pulverisation step, may be used as a feed for, for instance a coke oven. For instance a blend of filter cake below 0.5mm and smalls to 15mm or more may be used as a feed to a coke oven, in a steel works.

The handling of pulverised coal and of coal fines is liable to incur a flash hazard unless suitable precautions are taken and the addition of fine particulate polymeric material, especially of the very fine particle sizes and oil dispersions that are preferred, would be contra-indicated because of the fear of increased flash hazard. However the evidence available to us shows that there is no increased flash hazard and that it is easily possible to pulverise, store and transport the friable cake safely, using conventional techniques.

30 A particular problem arises when friable filter cake is transported by truck since the inevitable vibration during transport tends to cause permanent caking or packing of a product that is otherwise sufficiently friable to be homogeneously mixed with coal smalls.

Preferably therefore the friability is such that the *1 $r *s *r c a 0 *r 6 friable cake does not pack seriously into a truck during transport, and can instead be easily tipped out of the truck after transport.

The filter cake generally has a water content of to 40%, usually 25 to 35% and typically around 30%. The coal fines generally are substantially 100% below often mainly in the range 504m to 3004m and usually at least 80% by weight below l00m, for instance 64% below 604m. The ash content of the cake is usually below usually below 15%. The cake normally has the wet, sticky nature that is characteristic of conventional coal filter cake.

.4 The filter cake may have been stored for short periods in a truck) or for prolonged periods r 15 in a dump) before blending with the polymer, but preferably the filter cake is blended with the polymer substantially continuously after formation of the cake.

Cake formation is generally by vacuum filtration by a disc, drum or other vacuum filter of a slurry or froth flotation concentrate.

As mentioned above, it is known to convert a wet particulate mass into a friable form by mixing absorbent l •polymer particles into the mass, but the combinations of polymer, amount, particle size and mixing method that have been used previously would not have been effective S' for converting sticky coal fines filter cake into a friable form that can easily be blended substantially homogeneously with coal smalls. It has never previously 4 ,4 been appreciated that it is, in fact, possible to convert o 30 the sticky filter cake to a suitable able form by use of particular polymers and blending methods and that the resultant friable material can safely be pulverised with smalls or used in other ways as a feed for boilers, coking ovens or other purposes. It has also never previously been appreciated that the cake can be made so 7 V 11 l F r 7 friable that it does not seriously pack during transport but can instead easily be tipped out of a truck after transport.

If the cake has a friable form that can easily be blended substantially homogeneously with coal smalls, the friable cake will have a substantially uniform texture throughout and can easily be crumbled between the fingers either into the individual coal fines or into small aggregates of, for instance, less than about 5mm and generally less than about 2mm. These small aggregates can themselves readily be crumbled between the fingers into smaller aggregates and eventually into substantially individual coal particles. This texture must exist substantially uniformly throughout the product since if it is non-uniform, and there are sticky areas within the product, then these sticky areas will interfere with the blending and other operations to which the fines are to be subjected. This manual crumbling test is therefore an easy preliminary way of determining whether the cake is sufficiently friable.

A convenient way of ascertaining whether a particular dosage of a particular particulate polymer can a readily be used to provide the desired friable form is to a measure the dissociation time and the shear dissociation time of that polymer. dosage with the particular cake o, being used, For this purpose, the "dissociation time" is recorded by putting 600g of the coal filter cake in a Hobart mixer bowl, adding the water absorbent polymer, a 0and stirring at speed 2 until the product becomes S, 30 sufficiently friable that aggregates start being thrown out of the bowl. The time taken for this stage to be reached is the dissociation time and should generally be below 50 seconds, preferably below 30 seconds and most preferably below 15 or 20 seconds.

04 -jA 17'9 ?V 77V~ 8 After stirring for a further 2 minutes at speed 1, the resultant mix is left for 30 minutes in a sealed bag.

100 grams of the mix is put into a cylinder 65mm in diameter and pressed into this cylinder to a disc under a cake-forming pressure of 0.38kg/cm 2 (5.5psi) to give a cake. The cake is placed on a rectangular plate so that the entire cake is within the profile of the plate, but a substantially semicircular portion is cut away from one side of the plate so that about one third of the cake is unsupported. A solid plate is lowered at 12mm/sec on to the top of the cake by a piston and is pressed down on to it with a pressure of 5psi (0.35kg/cm 2 The time is measured between the plate touching the top of the cake I' and the cake shattering over the cut away part of the test plate. This is the shear dissociation time (SDT If the cake shatters immediately upon contact with the lowering plate, the shear dissociation time is recorded as zero.

SDT 5 needs to be below 30 seconds for generally satisfactory results and, in particular, if SDT 5 is below about 20 seconds, preferably below about 10 seconds and most preferably below about 7 seconds (especially "substantially zero) and if the dissociation time is satisfactory, then the polymer cake combination is such that, with appropriate mixing, homogeneous blendability with coal smalls can be expected. For instance Examples 1 and 2 below show that good results are obtained when SDT 5 is not above 7 and discussion is not above 18.

o For the friable cake to resist caking or clogging 30 during transport, a more friable texture is needed. For 0 4 i this, the SDT test is repeated under a cake-forming pressure of about 20psi (1.4kg/cm 2 to deteruine SDT or even at about 50psi (3.5kg/cm 2 to determine SDT These values also should be below about 20, preferably

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il:- L 8a below about 10, most preferably below about 7 seconds, especially substantially zero.

Having selected a potentially suitable combination of dosage, particle size and polymer type, it is then necessary to ensure that the polymer is mixed with the sticky cake under conditions such that the cake is converted to the desired friable form.

This requires, inter alia, that the mixing is thorough and rapid. The polymer must absorb water from the cake rapidly and uniformly. Most conventional mixing techniques are usually inadequate and, in particular, plug mixing must be avoided as this will leave sticky zones within the cake. Preferably 0*00 therefore the mixing involves some degree of back 0 mixing. This can be achieved by tumbling the mass along a conveyor but preferably mixing is by one 0 0 or more rotating members that provide both forward and back mixing and that provide adequate shear.

Preferred mixers are Simon or other double scroll mixers or, especially, plough share mixers. Suitable plough share mixers are Lodige Mixers or Morton or r Mixers. A plough share mixer has a substantially O 04 e horizontal cylindrical container provided with a coaxial rotating shaft that carries a plurality of mixing shovels each generally having the shape roact a of a plough share and mounted to rotate close to .o the wall of the cylinder. The peripheral speed and shape of the shovels causes the product to be o °0 whirled from the particulate mass in the lower part of the cylinder into the free mixing zone above the mass, so as to obtain high turbulence and both forward and back mixing.

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fee-lew-&bowte-l most preferably below especially substantially zero.

Having selected a potentially sui able combination of dosage, particle size and polymer/type, it is then necessary to ensure that the pol mer is mixed very thoroughly and rapidly with the/ sticky cake. The polymer must absorb water from/ the cake rapidly and uniformly. Most conventiona/ mixing techniques are usually inadequate and, in pa ticular, plug mixing must be avoided as this will le e sticky zones within the cake. Preferably theref e the mixing involves some degree of back mixing. Tis can be achieved by tumbling the mass along a conveyo but preferably mixing is by one or more rotating members that provide both forward and 15 back mixing and that/provide adequate shear. Preferred Sr mixers are Simon /or other double scroll mixers or, especially, plougt share mixers. Suitable plough share mixers are Lod' e Mixers or Morton Mixers. A plough 0 share mixer h s a substantially horizontal cylindrical a 20 container pr vided with a coaxial rotating shaft that carries a lurality of mixing shovels each generally having th shape of a plough share and mounted to rotate close to/the wall of the cylinder. The peripheral speed and sh pe of the shovels causes the product to be whirled 25 from the particulate mass in the lower part of the cylnder into the free mixing zone above the mass, so as Sto obtain high turbulence and both forward and back V° r The polymer can be added to the sticky mass by e 30 spraying or dusting, depending upon the form of the 0° polymer, and the mass then mixed in the defined manner.

Mixing should be continued for as long as is necessary to achieve thorough mixing, generally about 1/4 to minutes. The mixer preferably operates continuously.

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.7 A convenient way of determining whether the friability is such that the friable can be transported by truck and then tipped or poured out of the truck without substantial clogging or caking is by testing with a Durham Cone. A Durham cone is a cone of specified angle leading to an orifice of specified size incorporating a slide valve. The cone is filled with 10-20kg coal and vibrated at a fixed speed, the vibration is then stopped and the valve opened. If the friable coal fines flow evenly out of the cone, they are generally suitable for trucking without caking. If they flow unevenly and tend to clog, they are not suitable for trucking.

The polymer particles must be substantially non-sticky when wet in order that they do not cause permanent aggregation of the coal fines. The polymer preferably is substantially wholly insoluble (in the sense that very little, and preferably none, dissolves from the particles into the cake, and preferably L° substantially none dissolves from the particles upon stirring with water for 5 minutes). The polymerisation conditions and the monomers used for making the polymer are preferably such that the content of high molecular weight linear, or soluble, polymer is sufficiently low that during the process the particles do not become sticky. Typically the amount of polymer that would dissolve out of the particles during 2 hours contact with 0.9% aqueous saline solution is below 20%, preferably below The polymer is made from water soluble monomer or 30 monomer blend. The monomers are mainly 0 monoethylenically unsaturated, generally water soluble, monomers but cross linking agent is included in order to convert the resultant polymer to water insoluble but water swellable form. The cross linking agent can be reacted into the polymer after polymerisation but d homogeneousiy w±ll IInLL" 11 preferably is present during polymerisation. Generally it is a di- or other poly- ethylenically unsaturated monomer such as methylene bis acrylamide or any of the other ethylenically unsaturated cross linking agents that are suitable for cross linking absorbent polymer.

Instead of or in addition to relying on a covalent cross linking agent of this type, cross linking can also be through pendant groups in known manner. For instance it can be by polyvalent metal ions.

The polymer is made from 5 to 100% anionic or cationic monomer and 0 to 95% non-ionic monomer. The amount of ionic monomer is usually at least 10% by weight. The monomers are generally acrylic, but they can be allylic or other vinyl monomers.

Suitable anionic monomers are ethylenically unsaturated carboxylic or sulphonic monomers such as (meth) acrylic acid, allyl sulphonate or 2-acrylamido methyl propane sulphonic acid. Anionic monomers are generally present as a water soluble salt, usually a sodium salt. Alkali metal salts are especially preferred.

Suitable non-ionic monomers are (meth) acrylamide and Cl-4 alkyl (meth) acrylic esters, especially Shydroxyalkyl esters.

Suitable cationic monomers are dialkyl amino alkyl (meth) -acrylate or -acrylamide as free base, acid salt or, preferably, quaternary salt and diallyl dimethyl ammonium chloride.

Cationic monomers are generally used as a blend with acrylamide. The amount of cationic monomer in the blend is often about 10 to 60% by weight. Anionic monomers may be present as homopolymer or as copolymers of anionic monomer with, preferably, acrylamide.

The polymers can be as described in EP 213799, or cationic versions thereof.

to use anionic polymer alone.

The preferred anionic polymers are cross linked polymers of about 5 to 100 mole acrylic acid (as free acid or salt) with 0 to 95 mole acrylamide and optionally 0 to 50 mole other non-ionic or anionic monomer. The acrylic acid is preferably present as 12 With some filter cakes, best results are achieved using cationic polymer alone or blends of cationic 0 spolymer wit h anionic polymer, but it is often preferred to use anionic polymer alone.

80% by weight)red ani s sodium acrylate. Suitable polymers are copolymers of about 5 to 100 moule acrylic acid (asas free free acid or salt) is typically from about 10 or 20 to acid or salt) with 0 tothe balance being acrylamide. It is Sgeoptionally preferred0 to 50 mole other non-ionic or anionic monomers for the anincrylic polymeracid is preferably present as Typ sodium alt, wholly or mainly are crosst least 70 orinked polymers of about 40 to 60% by weight) as sodium acrylate. Suitable polymers are copolymers in which the amount of acrylic acid (as free acid or salt) is typically from about 10 or 20 to 60 to 40% by weighthe balance b acrylamide. It is Particularly preferred for least 40% by weight of the monomers for the acrynionic acidpolymer to b sodium salt homopolymers, Typical polymers of this general type are cross linked polymers of about 40 to 60% by weight sodium acrylate with 60 to 40% by weight acrylamide.

Particularly preferred swellable polymers for use in t the invention are acrylic acid sodium salt homopolymers, although up to 20% of the sodium acrylate can be replaced by acrylamide. Some of the acrylate groups usually are Sin the form of acrylic acid or other water soluble salts, generally other alkali metal salts.

The degree of swellability and absorption is S:I, controlled, in part, by the extent of cross linking and the amount of cross linking agent is usually below about 500ppm, often below 300ppm. It is usually at least 30 10ppm or 20ppm and preferably at least 50ppm. Best S results are often achieved at around 100 or 200ppm.

These amounts are the amounts by weight of monomer of methylene bis acrylamide and equivalent amounts of other cross linking agents may be used.

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(2z> C/C f 13 The degree of cross linking, and the polymer type, should be such that the gel capacity of the polymer (grams deionised water absorbed per gram dry polymer) is at least about 25, generally at least 100 and preferably at least 200 typically up to 500 or even 700 or higher.

In some instances it is desirable for the polymer particles to have a surface layer that is less swellable than the inner parts of the particles. The desired reduced swellability of the surface layer is preferably obtained by cross linking the surface layer. This reduces the content of linear polymer at any position where it might cause stickiness and has the advantage of promoting uptake of water and of preventing aggregation of the polymer particles. The desired surface cross linking can be achieved by methods such as those described in U.S. 3,114,651, 3,251,814, 4,043,952, 4,093,013 and 4,090,013, JP 1983/42602 and EP 227305.

Other ways of treating the surface are by applying a coating of a counter ionic polymer poly diallyl dimethyl ammonium chloride or other cationic polymer when the swellable polymer is anionic) or by applying sodium aluminate or other aluminate.

The polymer particles can be relatively large, e.g., up to 0.5mm or even 1mm or up to 2mm, but the degree and duration of mixing that is necessary generally increases 1 as the particle size increases. For most purposes it is 1 'f therefore generally desirable for the particles to have a size during the mixing step of below 300m and generally below 2004m and preferably at least 90% of the particles 30 have a size during the mixing step below 504m. However o when the greatest degree of friability is required to resist cdking during trucking) it is surprisingly best to use larger particles 100-3004m or even up to 1 or 2mm) with sufficiently prolonged mixing.

'4 I 4i #4 *1 441- In particular we find with conventional cominuted or bead polymer particles that, as the polymer size increases, potential friability can increase and the risk of polymer overdosing decreases. At lower particle sizes below 125gm), adequate friability for homogeneous blending with coal smalls can be obtained in the invention. However caking may be a problem during trucking of the friable product due to it being insufficiently friable to resist the effect of vibration SDT 5<10 but SDT 20>20 seconds). Mixing can be fairly quick (dissociation below 20 seconds), but friability is very dose sensitive in that SDT deteriorates quite markedly either side of a fairly narrow range of optimum doses. At coarser particle 15 sizes, greater doses and longer mixing times are needed (dissociation times up to 50 seconds and sometimes even up to 120 seconds) but the friability is better (SDT seconds and often <10 seconds) and there is less risk of overdosing.

The polymer particles may be introduced as individual particles having the size that is requifed during the mixing step or they may be introduced as aggregates that we assume break down during the mixing step into smaller particles that have the desired size during the mixing.

If particles below 504m are introduced into the mixing step in the form of free powder, the handling of the particles can cause dusting problems and the system is dose sensitive and SDT 20 may be rather high. We 30 have surprisingly found that it is possible to combine the lower dosages and the fast mixing characteristics of small particles with the improved friability and reduced risk of overdosing, and avoidance of dusting problems, of large particles by introducing the polymer in the form of powder having a particle size above 50gm and which 4 4 1 1 4 a D a 4 a a a i,.

a,:l 2-f consists of internally bonded aggregates of finer particles having a size of below 50m and often below For instance polymer gel fines, as obtained from the comminution of polymer gel or as fines from a reverse phase bead polymerisation process, can be aggregated by swelling with sufficient water to form a comminutable gel, comminuted to a coarse size and dried by a fluidised bed). These internally bonded aggregates appear to behave initially as coarse particles and then to behave as fines.

Any aqueous solution that permits swelling can be used. Water is usually best. An aqueous solution of a small amount of a soluble polymer or other binder could be used. The comminution can be to >90% by weight above 50gm and usually above i00m, but generally below 1 or 2mm and often below 500gm. Comminution can be by conventional gel comminution methods. Drying can be by conventional techniques followed if necessary by comminution in conventional manner. The resultant aggregates have a size in the range generally of 50 to 5004Am. They can very satisfactorily be used in the invention. The fines within each aggregate typically have a size mainly 5 to 304m and often below By swelling the fines into a comminutable gel, the resultant dried comminuted particles appear to be internally bonded. This is in contrast to the skin bonding effect that is obtained if fines are merely sprayed with water and immediately dried in a fluid bed.

Skin bonded aggregates can be used in the invention but S 30 internally bonded aggregates give better results. They are novel materials.

Another effective way of incorporating the preferred particles having at least 90% by weight below 50m is as a dispersion in water immiscible liquid.

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Z knbne grgtscnb sdi h neto u 16 Preferably at least 90% of the particles are below about 20am or 304m, and most preferably below Fastest results are generally achieved with at least preferably 99%, by weight being below 34m, in the range 0.03 to 24m. Often however adequate results are obtained in a cost effective manner, albeit more slowly, if the particle are 90% between 5 and 50gm, about to 304m.

Whereas most industrial processes that use dispersions of polymer in water-immiscible liquid require that the amount of polymer should be as high as possible, in the invention we find that best results are achieved when the amount of polymer is relatively low. Thus although the dry weight of polymer can be up to, for instance, 50 or 60% by weight of the dispersion, the dry weight of polymer in the dispersion is preferably below by weight and preferably below 40%. Generally it is I at least 15%, preferably at least 20%. Concentrations of 30 to 40% polymer dry weight based on total dispersion are often best when the polymer particles are wet and to 30% when the polymer particles are dry.

The water-immiscible liquid may be any organic liquid in which the polymer particles can be adequately .'0l dispersed and that will not interfere with the process *o 25 and so in practice needs to be substantially water Simmiscible. It can be, for instance, a vegetable oil but is preferably a hydrocarbon or halogenated hydrocarbon liquid. It may be selected from any of the i, liquids conventionally used in reverse phase dispersions.

0 30 For instance it can be kerosene or diesel oil or other mineral oil.

The dispersion can be formed at the point of use, with the polymer particles being dispersed into the water-immiscible liquid and the mixture then being applied substantially immediately to the wet particulate

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17 mass. Preferably however the dispersion is preformed, in which event it needs to be substantially stable against settlement.

One form of dispersion is a suspension obtained by dispersing preformed dry polymer particles into water-immiscible liquid in the presence of a dispersion stabiliser. The preformed dry polymer particles can be reverse phase microbeads but preferably they are fines separated from polymer gel, obtained during the comminution of bulk or bead gel or separated from beads obtained by reverse phase polymerisation.

The amount of stabiliser is generally from 1 to often 3 to 10%, by weight based on the dry weight of polymer. Conventional stabilisers for oil based dispersions may be used, Bentone clays but preferably the dispersion is stabilised by stirring into it an aqueous emulsion of an oil soluble or oil swellable polymeric thickener, generally a thickener that is insoluble and non-swellable in water. Suitable thickeners are described in EP-A-0161926, for instance in Example 7 and at page 11 line 22 to page 12 line Instead of using polymer fines, typically having a size of 10 to 30 or 10 to 404m, the dispersion can be a reverse phase dispersion made by reverse phase polymerisation of aqueous monomer or monomer blend in water-immiscible liquid. See for instance U.S.

4,059,552. The reverse phase polymerisation is preferably conducted as a reverse phase suspension I -i1 polymerisation. Formation of an initial dispersion of l 30 monomer particles can be facilitated by the incorporation of a small amount of water-in-oil emulsifying agent.

Often amphipathic stabiliser is included, in known manner, especially when the dispersion is subsequently azeotroped. Depending upon the degree of agitation when forming the initial dispersion of aqueous monomer in the S 0* i *i i lrev i i

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i s: i i- ^r'l? non-aqueous liquid, and depending upon the amount and type of stabiliser and emulsifier, if present, the dry particle size of the final dispersion can be controlled and typically has a maximum size of l4m or up to 2 or 34m or lOm at the most. The product of the reverse phase polymerisation can be described as an emulsion. It may be dried, by azeotroping to reduce the water content, typically to below 15% by weight of the polymer.

The product is then a substantially dry dispersion.

The amount of amphipathic stabiliser (if present) is generally in the range 0.2 or 0.5 to 10%, and generally below based on the weight of polymer. The amount of water-in-oil emulsifier is preferably from 0.2 to 3%, based on weight of monomer.

In normal processes in which a dispersion in oil of water soluble or swellable polymer is mixed into water, it is conventional to conduct the mixing in the presence of an oil-in-water emulsifier so as to promote distribution of the dispersion and the dispersed polymer into the water. For instance, it is common to add the emulsifier to the polymer dispersion before blending with the water. Because of the apparent need to achieve rapid distribution of the polymer throughout the wet particulate mass, we therefore expected it to be necessary to use such an emulsifier. We have surprisingly found, in the invention, that better results are achieved in the absence of this emulsifier than when the conventional addition is made. This suggests, surprisingly, that it is desirable to retard the rate at which the polymer particles are made available to, and can take up water from, the wet filter cake.

Since one purpose of the polymer particles is to absorb water from the wet filter cake it would be expected that the particles should be as dry as possible at the start of the process. However we have

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t oi 0 ow a 0 00 surprisingly found that improved results are achieved when: at the time of addition to the wet particulate mass, the polymer particles in the dispersion contain a substantial amount of water, usually at least 30% based on the dry weight of polymer. Usually the amount is below 150% and typically is in the range 60 to 120%, preferably 80 to 100%, based on the dry weight of polymer.

Preferred compositions comprise 20 to 50% by weight of each of the polymer (dry weight), water-immiscible liquid and water. The amount of each of the polymer and the water immiscible liquid is preferably 25 to 45%, most preferably 30 to 40% by weight. The amount of the water is preferably from 20 to 40%, most preferably 25 to Particularly preferred compositions comprise 30 to 40% by weight polymer, 30 to 40% by weight water immiscible liquid and 25 to 35% by weight water, with the amount of water generally being less than the weight of polymer.

Compositions containing such amounts of water tend to be unstable if the dry particle size is significantly above 10m and so the preferred compositions that contain water have a particle size lower than this, preferably below 3C4m. They can be made by reverse phase polymerisation (usually by reverse phase suspension polymerisation) to form an emulsion of aqueous polymer gel particles dispersed in the water immiscible liquid, and then the emulsion can be used as such without further drying and without the addition of oil-in-water activator. However for some purposes it appears best to dry the emulsion by azeotroping in conventional manner and then to add water back into the dispersion.

It is very surprising that better results can be achieved using wet polymer particles than dry, both because it would be expected that dry particles would be more effective absorbents and because it has occasionally 71 1' Ie "9v ?P II .I _i j been suggested in the literature that wet particles initiate absorption quicker than dry particles. However the improved results obtainable in the absence of oil-in-water emulsifier indicate that accelerated absorption is not desirable.

When the polymer particles are large, such that the swollen polymer particles have a size greater than the size of most or all of the coal fines, the swollen polymer particles can subsequently be separated from the dry coal fines. For instance in one process according to the invention at least 50% (dry weight) of the swollen polymer particles have a size greater than the size of at least 95% of the substantially dry coal fines and these oversize swollen particles are separated from the dry coal fines. Preferably the polymer particles swell to d at least twice their dry diameter and substantially all the said swellen polymer particles have a size greater than the size of substantially all the dry coal fines and the polymer particles are separated from the dry coal fines. The separation may be .by conventional size classification or weight classification techniques, us' preferably by seiving using a vibrating seive.

The dry coal fines are subsequently used as fuel and as a result of having separated the polymer from the fines the water content of the polymer is not carried in t l to the fuel and the separated swollen particles can, if desired, be dried by heat exchange from the fuel burner) and can be recycled for further use.

The swellable polymer particles may be mixed with the wet filier cake without any prior addition of any Bo material to the filter cake. However improved results a 0 can be achieved if the filter cake that is mixed with the o o swellable polymer particles have previously been treated with a co-ionic dispersing agent, a counter-ionic coagulant, or a co-ionic, counter-ionic or non-ionic 1 W i> 21 flocculant. ("Counterionic" means that the agent is cationic when the swellable polymer is anionic, and vice versa.) For instance the wet filter cake may be blended with a solution of the dispersing agent, coagulant or flocculant so as to promote liberation of bound water from the cake, before adding the absorbent polymer particles. In some instances it can be desirable to include the dissolved agent with the coal fines at the time of a filtration stage, for producing the wet filter cake. For instance a slurry or froth concentrate of the coal fines can be treated by a coagulant or a flocculant or a combination (usually a coagulant followed by a flocculant) prior to filtration to provide the wet filter cake.

Co-ionic dispersing agent is generally a polymer of low molecular weight, usually below 500,000, generally below 200,000 and often below 50,000. For many processes molecular weights of below 10,000, 2,000 to 5,000, are satisfactory. The dispersing agent is usually anionic. The counter-ionic coagulant generally has a molecular weight of above 50,000, often in the range 100,000 to 1 million, typically about 500,000.

However it can have a higher molecular weight. The flocculant can have molecular weight below 1 million but generally it is above. It can be of several million, and can be of typical flocculant molecular weight.

Although these polymeric agents are usually substantially linear and are applied in true solution, it j can be particularly advantageous, especially when the agent is a higher molecular weight agent such as a flocculant, for the agent to be in the form of very small particles at the time it is mixed with the wet coal o fines, preferably being a slightly cross linked flocculant polymer. For instance it may be as described in EP 0202780.

A Ao 1- 22 The added agents are usually synthetic polymers formed from water soluble ethylenically unsaturated monomers, and these monomers will be chosen to give the polymer the desired ionic characteristic. They may be any of the anionic, cationic and non-ionic monomers listed above for the swellable polymer. The cationic dispersing agent is preferably a low molecular weight polymer of diallyl dimethyl ammonium chloride or dimethyl amino ethyl (meth) acrylate, or a blend of either of these with acrylamide.

It is often preferred that the particle sizes and the amounts of the absorbent polymer and of the filter cake are such that the number ratio of swellable polymer particles:filter cake particles is approximately 1, e.g., from 3:1 to 1:3. For instance this is achieved by adding about 0.2% (dry on dry) of polymer particles having a particle size of about 20 to 30m to filter cake having a particle size of about 004m. Larger amounts of these polymer particles are appropriate when the filter cake has a significant electrolyte content.

The amount of absorbent polymer that is applied is generally at least 0.005% and is preferably at least 0.05%. It is usually below preferably below 1% and most preferably is around 0.05 to It is a particular advantage of the invention that, despite the unpleasant sticky character of the filter cake, good Sresults can be obtained with very low amounts of polymer, ,O often below 0.3% or 0.4% and often below 0.15% or 0.2%.

These amounts are of dry polymer based on dry particles 30 by weight.

0 The following are some examples.

o Example 1 SSodium polyacrylate cross linked with 0.025% methylene bis acrylamide is formed by conventional bulk gel polymerisation and is dried and comminuted in a Ac, ~ic E 1 classified according to size and the fines are retained for use in the invention. They have a dry particle size below 504m, mainly in the range 10 to 304m.

The fines are dispersed into an equal weight of a hydrocarbon oil that is thickened with a dispersion stabiliser as described at page 18 lines 25 to 35 of EP 0161926A. 1% oil-in-water emulsifier is included.

The dispersion is sprayed on to a wet filter cake of coal fines, this filter cake having been taken from a vacuum filter following froth flotation. The amount of dispersion is 0.1% dry polymer on dry particulate mass.

The product is mixed thoroughly and rapidly becomes a friable, crumbly solid. This can easily be blended with coal smalls to form a fuel. Without the addition of the dispersion, the filter cake is a wet sticky mass that could not easily be used.

In a comparison, when a similar amount of dry polymer particles of the same polymer but having a size of around lO04m, and that are not dispersed in oil, was added to the cake, the cake does not become so crumbly so quickly. With prolonged mixing and larger amounts of polymer 0.2% or even the product is adequately crumbly but swollen polymer particles and aggregates are apparent.

Three types of dispersion, each containing equal oamounts of polymer and hydrocarbon oil (kerosene or diesel), and oil-in-water emulsifier, are made as follows.

o Suspensions by the general technique of Example 1 using particles of the size shown, with >90% by weight J RP Emulsions by the reverse phase polymerisation to give a product of about 35% oil, 35% polymer, 30% water n t. o f

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i i7!nri i: I, -L i .r 1 24 RP Dispersions by azeotroping RP Emulsions to about polymer 50% oil The compositions are tested at 0.5% product on wet coal filter cake as above. The monomers used and the results are in the following table, where NaAc sodium acrylate, ACM acrylamide and MBA methylene bis acrylamide (ppm).

Ccposition NaAc ACM MBA Dissociation SDT Ex 1 100 0 200 18 7 355-500wm Suspension 50 50 200 82 0 65-180im Suspension 50 50 200 28 0 Suspension 50 50 200 14 0 RP Dispersion 50 50 100 50 0 do. 50 50 200 37 O do. 50 50 300 75 0 do. 25 75 25 30 do. 25 75 50 42 11 do. 25 75 100 32 0 do. 25 75 200 40 0 RP Emulsion 100 0 100 31 4.2 RP Dispersion 100 0 100 25 14 It is apparent from this that some of the 30 exemplified processes require rather long mixing times because the dissociation time is rather high for satisfactory results. However it is also apparent from these examples that it is easy to achieve satisfactory results by, for instance, reducing the particle size from I0 It 44 4 4 *4 I O 04 o CE J~ .21i Fmir uuf I: above 355&m to below 180gm or by increasing the proportion of sodium acrylate. It is also apparent that if the amount of cross linking agent is too low (25ppm in this example), SDT 5 is too high. This is probably due to the polymer containing too much soluble polymer, thus rendering it sticky.

Example 3 Tests similar to Example 2 are conducted on RP dispersions of 50% oil and 50% of a copolymer of 50% NaAc ACM 200 ppm MBA with or without added oil-in-water emulsifier, at different amounts of polymer.

Dispersion Amount Emulsifier Dissociation SDT 0 16 O 0.2% 0 25 1.8 0.5% 3% 23 O 0.2% 3% 37 2.2 The disadvantage of incorporating emulsifier is apparent.

Example 4 Tests similar to Example 2 are conducted on a 50% RP dispersion of a copolymer of 50% NaAc 50% ACM 200 ppm MBA (product A) and the same product after dilution to polymer by red diesel oil r c

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LIJ I i 26 Dispersion Polymer Amount Concentration Dissociation SDT 0.5% A 0.3% A

B

0.6% B 50% 50% 25% 25% 19.4 30.1 14.8 22.3 2.6 11.0 2.3 7.9 The benefit of reducing the polymer concentration is apparent.

Example A RP dispersion is formed of 50% oil 50% copolymer of 50% NaAc 50% ACM 200 ppm MBA. This is diluted with various amounts of water and the products are tested on wet coal filter cake as in Example 2 at different dosages of product.

Product Amount Polymer Water Oil Dissociation SDT 50 0 50 19 3.4 0.2% 50 0 50 31 0.56% 45 10 45 31 4.8 0.22% 45 10 45 34.6 10.6 0.63% 40 20 40 24.9 3.8 0.25% 40 20 40 31.8 8.9 0.71% 35 30 35 24.1 2.4 0.29% 35 30 35 29.9 14.4 0.83% 30 40 30 22.5 2.9 0.33% 30 40 30 26.8 1.0% 25 50 25 22.6 3.9 0.4% 25 50 25 29.7 This clearly shows that the addition of a controlled

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4P amount of water gives improved results at low dosages and thus provides a particularly cost effective system.

Example 6 Example 2 is repeated using similar amounts of three different polymer suspensions. Tests 2-4 are with dispersions in oil and tests 5-7 are with 50% dispersions in oil. Test 8 is with 1% of a 25% emulsion of aqueous polymer particles in oil and test 9 with a 50% dry dispersion of similar, but dry, polymer particles. The unsatisfactory results from non-ionic polymer are shown in test 7.

Test Polymer ppm MBA Amount Dissociation SIT 1 100 NaAc 200 0.5% 18 4.6 2 25 NaAc 75 ACM 100 0.4% 20.3 3.4 3 20 NaAc 80 ACM 100 0.4% 25.6 2.6 4 10 NaAc 90 ACM 100 0.4% 29.8 2.4 50 NaAc 50 ACM 200 0.5% 37.6 O 6 25 NaAc 75 AQM 200 0.5% 40.5 0 7 100 ACM 200 0.5% 39.4 8 50 NaAc 50 ACM 100 1% 23.0 3.9 9 50 NaAc 50 ACM 100 0.5% 22.4 2.9 Example 8 The process of example 2 is repeated but using a by weight RP emulsion in oil of cationic swellable polymer formed from 60% ACM 40% dimethylaminoethyl acrylate (MeC1 quaternary salt). At 1% dosage, Dissociation is 11.7 seconds and SDT 5 is 0.9. When using a 1% polymer dosage of a 50% RP dispersion of a swellable polymer of 50% ACM 50% NaAc (instead of the cationic polymer). Dissociation is 11 and SDT 5 is 1.2.

Example 9 An aqueous solution of cationic soluble polymer A, B or C is stirred into a wet filter cake of coal fines.

After stirring for one minute, a 50% dispersion in oil of 4 .4 a Ie 64 1 66 4r 0c 4 4 y 664 0 00 66 66 y 01 66 66B 66 6 -4 V

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'X I vW 0 Li.': I I II ii~i.hiii4Li 28 cross linked gel polymer particles of acrylamide and sodium acrylate polymer is blended into the filter cake.

The results are as follows, in which polymer A is a low molecular weight diallyl dimethyl ammonium chloride coagulant, polymer B is a high molecular weight, slightly cross linked, copolymer of 58 mole percent acrylamide and 42 mole percent cationic dialkylaminoalkyl acrylate quaternary monomer, and polymer C is a homopolymer of a cationic dialkylaminoalkyl methacrylate quaternary monomer. In addition to the results shown in the table below, the product was assessed visually and it is significant that increasing amounts of product B, and especially the tests with product C, give the best visual appearance.

Cationic Dispersion Dissociation SDT Polymer 0.05 A 0.15 A 0.15 A 0.3 A 0.5 0.5 1.0 1.0 1.0 1.0 18.4 19.6 17.5 .17.5 16.9 15.2 17.5 12.1 10.9 17.5 6.7 3.1 3.6 2.6 0 1.9 2.6 0 2.6 0.08 B 0.16 B 41 g 4.

814i 0D 0 14 0 44. 14 4 Ip 0 44 O 0.4 C 1.0 8.7 0 0.8 C 1.0 8.6 0 Example Fines having a size mainly 10-304m are separated from comminuted cross linked polyacrylic acid (75% as sodium salt) gel having a gel capacity well in excess of 25g/g. They are labelled A. Part of them are mixed with sufficient water to make a comminutable gel which is then comminuted and dried on a fluid bed drier, in r 9;

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L -illlllL~lY~i conventional manner, to a particle size >1254m but below 500pm. This is labelled B. Each product is mixed with coal filter cake as in Example 1 at various doses.

Product Product Dose Dissociation Time (sec) SDT 5 SDT 20 SDT A 0.25 13.1 2.7 30+ 9.9 1.3 4.7 0.75 8.3 0.7 2.9 7.9 0.9 2.9 B 0.25 23.2 1.5 14.8 0 2.0 0.75 13.1 0 0 3.6 12.5 0 0 2.1 This demonstrates that the agglomerates give improved results at higher dosages but give similar results at lower dosages.

Example 11 Products A, B and C are formed from 50% ACM 50% NaAc cross linked swellable polymer having gel capacity above A is a dispersion in oil of particles <40 m. B is powder <63m and C >1254m. Different amounts are blended as in Example 1. The results are as follows.

t& a 1 "Ur o o 0 C 0 0 a S* 1- i; I Product Active Dissociation SDT 5 SDT 20 SDT Dose Time (sec) A <40mn 0.15 0.25 0.75 15.6 12.5 9.8 8.1 7.4 5.9 2.7 1.7 2.4 2.7 B <63pm 0.15 20.8 0.25 12.2 2.7 8.9 1.2 3.1 0.75 8.2 0 3.5 7.2 0 3.8 6.6 0 3.9 C >125pm 0.15 25.4 0.25 15.7 .1.0 5.6 10.9 0 0 0.75 9.5 0 0 0.8 9.3 0 0 0.8 7.5 0 0 0 This again shows that low particle sizes give satisfactory dissociation and SDT 5 values at low dosages but inadequate SDT 20 values, but also shows that there is an optimum low dose. It also shows that although large particle sizes give good SDT 20 and SDT 50 values at high doses, the results are not acceptable at lowest doses. Also the benefits of the large particles are not lost when the dose is increased further. Comparison with Example 11 shows the benefits of using agglomerates rather than conventional particles of similar size.

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Anionic Product Dissociation SDT 5 SIT 20 SDT Dose Time (sec) 3% 0.15 0.25 15.8 14.5 2.5 13.0 0 0 0.15 13.6 1.9 0.25 11.2 0 2.1 10.0 0 0 2.1 9.1 0 0 1.7 100% 0.15 14.7 0 0.25 12.2 0 0 11.7 0 O O 9.7 O O 0 This clearly demonstrates that the non-ionic product gives, at equivalent dosage, greatly inferior results compared to the more highly anionic grades used in the invention.

Example 13 Polyacrylic acid (about 75% in sodium form) gel cross linked with about 200ppm MBA is formed, comminuted and dried in conventional manner. Fines having a size mainly in the range 10 to 40pm are separated and dispersed at 50% solids in kerosene or diesel using an It o 0 oa o 0 0a 0 I 00 0~ 08 a'.

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32 emulsion of stabilising polymer (as in EP-A-0161926, Example 7) as stabiliser.

The resultant dispersion is diluted to about solids with further kerosene or diesel and sprayed at about 0.2% polymer on to coal filter cake having a coal size mainly 50 to 150m and a moisture content around and an ash content of around 10% as the cake is fed into a continuously moving Lodige Plough Share mixer.

The mix passes through the mixer in not more than about 2 minutes and emerges as a friable product that can easily be crumbled between the fingers (the SDT 5 for the wet filter cake-polymer combination is below The friable product is blended with about 5 times its own weight of coal smalls having a size of 1 to and the mix is pulverised and carried, entrained in air from the pulverisers, as a fuel into the combustion chamber of a power station boiler. There is no evidence of clogging of the pulverisers or other parts of the apparatus through which the product travels from the mixer to the boiler.

The blend, before pulverisation, may flow evenly out of a Durham Cone at that is uniform and is about 1.4kg/sec, whereas the untreated cake clogs or flows r o or unevenly at about half that rate.

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Claims (20)

1. A process for making a non-sticky, combustible, fuel from sticky coal fines filter cake comprising mixing particulate absorbent polymer into the cake, characterized in that the polymer is a non-film forming, cross linked, synthetic polymer that has a gel capacity of at least 25 grams deionised water per gram polymer and that is formed from water soluble ethylenically unsaturated monomer or monomer blend of which at least 5% by weight is ionic and the polymer is in the form of particles that are substantially S, non-sticky when swollen by water, and the mixing is conducted under conditions such that the cake of t is converted by the mixing from its sticky state ,to a friable form that can easily be blended substantially homogeneously with coal smalls.

2. A process ccording to claim 1 in which the resultant friable mass is blended with coal smalls.

3. A process according to claim 1 or claim 2 in which the polymer is mixed into the cake by one or more rotating members that provide both forward 0 and back mixing and that provide shear and the amount of ionic monomer is at least 10% by weight. o000 4. A process according to any preceding claim in S which the polymer is a cross linked polymer of to 100% by weight acrylic acid sodium salt and 0 to 90% by weight acrylamide. AU cot ®-4 N 0 C Kcey 33a A process according to claim 4 in which the polymer is formed of 80-25% by weight acrylamide and 20-75% by weight acrylic acid sodium salt.

6. A process according to any preceding claim in which the surface of the polymer particles is preferentially cross linked.

7. A process acording to any preceding claim in which the polymer particles have at least 90% by weight below 50,m and are added to the cake in the form of a dispersion in water immiscible liquid. Q at at C *e i a I t r a t I t a It *J J'. 34

8. A process according to claim 7 in which the dispersion is a dispersion of fines obtained from polymer gel.

9. A process according to claim 8 in which the dispersion is stabilised against settlement as a result of the incorporation into the dispersion of an oil swellable or oil soluble polymeric thickener. A process according to claim 7 in which at least by weight of the polymer particles have a dry size below l0gm and the dispersion has been obtained by reverse phase polymerisation.

11. A process according to any preceding claim in which the particulate polymeric material, its amount and the filter cake are such that the dissociation time, as S 15 defined herein is not above 18 seconds and SDT 5, as defined herein, is not above 7 seconds.

12. A process according to claim 7 in which at least by weight of the particles have a dry size below 10im and a dispersion contains at least 30% by weight water.

13. A process according to claim 7 in which the dispersion is made by reverse phase polymerisation and comprises. 25 to 45% by weight of the polymer particles, ao 407, to by weight water and 25 to 45% by weight water immiscible liquid, and the polymer particles have a dry size below

14. A process according to claim 7 in which the 1 dispersion is substantially free of oil-in-water h emulsifier. A process according to any preceding claim in which the mixing is by a double scroll or plough share mixer. 2 16. A process according to any preceding claim in which the mixing is conducted substantially continuously using a plough share mixer.

17. A process according to any of claims 1 to 6 in which the polymer particles are added to the mixture while having a size mainly above 125im.

18. A process according to claim 17 in which the polymer particles are added to the mixture as internally bonded agglomerates having a size mainly above 125Im and formed of fines having a size mainly below 304m.

19. A process according to claim 17 or claim 18 in which SDT 20, as herein defined, is below

20. A process according to any of claims 17 to 19 in which the mixing is by a plough share mixer.

21. A process according to any preceding claim in which the particulate polymeric material, its amount and the filter cake are such that SDT 5, as defined herein, is 15 below 20 and dissociation, as defined herein, is below seconds.

22. A process according to claim 21 in which the polymer 1 particles have at least 90% by weight below 504m and are added to the cake in the form of a dispersion in a water immiscible liquid.

23. A process according to any preceding claim in which the filter cake is taken from a stack of dumped filter cake.

24. A process according to any of claims 1 to 22 in which the filter cake is taken off a filter as the cake is formed. A process according to any preceding claim in which the friable product is blended with coal smalls in an amount of at least 10% and the blend is pulverised and carried in an airstream, optionally after storage, into a 0 combustion chamber where it is burnt. S o 26. A process according to claim 1 substantially as herein described with reference to any of the Examples. Z 23 ii- I., e -1 6= L ,G a= r sanG 1113 ff-2toKff- to or indicated in the specificat' or claims of this application, indivi. or collectively, and any and all w w Dated this 23rd day of March 1988 ALLIED COLLOIDS LIMITED By its Patent Attorneys DAVIES COLL1SON o II 4 041 441

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