AU695974B2

AU695974B2 - Waste paper treatment process

Info

Publication number: AU695974B2
Application number: AU50647/96A
Authority: AU
Inventors: Ian Stuart Bleakley; Hannk Olavi Ensio Toivonen
Original assignee: ECC International Ltd
Current assignee: Imerys Minerals Ltd
Priority date: 1995-04-13
Filing date: 1996-04-12
Publication date: 1998-08-27
Anticipated expiration: 2016-04-12
Also published as: GB9507716D0; GB9513701D0; AU5064796A; GB2300564A

Description

AUSTRALIA

Patent Act COMPLETE SPECIFICATION

(ORIGINAL)

Class Int. Class Application Number: Lodged: Complete Specification Lodged: Accepted: Published: Priority: Related Art: Names(s) of Applicant(s): ECC INTERNATIONAL LIMITED Actual Inventor(s): 9.

S S S. 55..

S

S.

lan Stuart Bleakley Hannk Olavi Ensio Toivonen Our Address for service is: PHILLIPS ORMONDE FITZPATRICK Patent and Trade Mark Attorneys 367 Collins Street Melbourne, Victoria 3000, Australia Complete Specification for the invention entitled: WASTE PAPER TREATMENT PROCESS Our Ref: 448478 The following statement is a full description of this invention, including the best method of performing it known to applicant(s): -1- 2210x -1ft- WASTE PAPER TREATMENT PROCESS This invention relates to a process for treating waste paper and, more particularly but not exclusively, is concerned with a process for recovering a useful product from suspensions, or slurries, which contain particulate material and which are derived from a plant for treating waste paper, for example a plant for deinking printed waste paper, de-inking plant waste being especially difficult to treat.

A process for converting waste paper into a pulp suitable for re-use will often include one or more operations designed, for example, to separate printing ink from the cellulosic fibres in the waste paper.

Generally, in a plant for de-inking waste paper, the waste paper is first pulped, for example in a pulper provided with a low attrition rotor, in water containing various chemical reagents, at a consistency which is usually in the range from about 8 to about 18% by weight of dry waste paper. The chemical reagents used generally include sodium hydroxide which causes the fibres to swell and saponifies most commonly used printing ink vehicles, sodium silicate which acts as a pH buffer and agglomerates detached ink particles to a convenient size, and a surfactant which aids wetting 25 and dispersion of the ink particles. The pulper is generally operated at a temperature in the range from 55 to 70 0 C and at a pH in the range from 9 to 11. On completion of the pulping operation the pulp is usually diluted with water to about 4 5% by weight of dry 30 solids and then reconcentrated to a consistency of about 14-16% by weight of dry solids: the dilution and subsequent reconcentration is advantageous because the dilute suspension is easier to pump from the pulper to 5 the next stage, and because it makes it possible to 35 return a proportion of the hot water and chemicals to the pulper.

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-2- The pulp suspension is then passed to a system of screens which remove relatively heavy foreign bodies, such as staples, paper clips and particles of grit, and also light-weight contaminants, such as plastics materials, and "stickies" which arise from adhesives used in paper coating, binding or laminating, and from hydrophobic reagents, such as sizing agents.

The suspension passing through the screens is then fed to a treatment plant which usually comprises one or more froth flotation cells, or one or more washing units, or a combination of flotation cells and washing units.

For example, a typical treatment plant might comprise one or more froth flotation cells, each of which is provided with an impeller and means to introduce air in the form of fine bubbles in the vicinity of the impeller. An additional chemical, known as a collector, is added to the pulp suspension prior to the flotation operation. The collector may be, for example, a fatty acid soap or a nonionic surfactant such as an ethylene oxide/propylene oxide copolymer.

The collector attaches itself preferentially to the ink particles, rendering them hydrophobic, so that they have greater affinity for the air bubbles than for the 25 water, and are lifted to the surface by the bubbles as they rise through the suspension. It may be necessary, in order to provide a sufficiently stable foam, to add also a water-soluble calcium salt to ensure that the water has a hardness of at least 200mg of CaCO 3 Ink 30 particles having sizes in the range from about 20Am to about 200Jm are concentrated in the froth which overflows from the top of the flotation cells, while a pulp suspension depleted in ink is withdrawn from the .bottom. The pulp suspension from the bottom of the 35 flotation cells is then washed with water, and subsequently dewatered, to remove as much as possible

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-3of the remaining ink residue. The dewatered pulp is then generally dispersed with a surfactant, which may be, for example, of the nonylphenol ethoxylate or ethoxylated alcohol type. The dispersion is effected by treating the mixture of pulp and dispersing agent with steam tc raise its temperature to a value within the range 50 90 0 C, and subjecting the hot mixture to intense mechanical agitation whereby remaining ink particles are generally reduced in size to below about 20gm, at which size they remain in suspension and become invisible to the naked eye. The pulp containing finely dispersed ink particles is then passed through a fine slotted screen to remove any agglomerates or remaining sticky or resinous material and finally dewatered to produce a substantially de-inked pulp. The water recovered from the dewatering operations is generally cloudy as a result of its content of fine particulate material which may comprise, for example, inorganic filler particles or organic particles such as ink or fine fibres. It is necessary to remove as much as possible of this particulate material before this water is suitable for recycling for use in earlier stages of the de-inking process. The cloudy water may be cleaned, for example, in microflotation cells in 25 which fine bubbles of air are injected at the base of the cells and the particulate material is carried upwards by air bubbles which attach themselves thereto, and is discharged at the top of the cells in the froth.

The treatment plant reject, which is usually in 30 the form of a suspension, or slurry, comprising the froth product from a flotation stage or the suspension that has passed through the screen of a washing stage, generally contains, in addition to the ink particles, a substantial proportion of the inorganic filler o 35 particles which were originally present in the waste paper. These filler particles generally consist predominantly of a mixture of kaolin clay and calcium carbonate in various proportions, although other inorganic filler particles such as talc, calcium sulphate or titanium dioxide may also be present in minor proportions. Hitherto, this treatment plant reject has had to be discarded as waste because of its very dark colour as a result of its high content of printing ink residues. There has, therefore, been a loss to the paper maker of potentially useful inorganic particulate materials. Also, the paper maker has had to meet the expense of disposing of the treatment plant reject in a manner which has no undesirable effects on the environment.

According to the present invention there is provided a method of treating reject from a plant for de-inking waste paper which reject comprises a mixture of ink particles, inorganic particles and fibres which includes the step of forming in an aqueous suspension or slurry comprising said reject a precipitate of a substantially white insoluble salt which entrains or aggregates ink particles, inorganic particles and fibres contained in said reject whereby the darkness of the reject is reduced by formation of the precipitate.

The precipitated salt preferably comprises a salt which S shows a neutral pH in an aqueous solution. Preferably, the salt comprises one or more alkaline earth metal carbonates although it could alternatively or in addition comprise one or i more of aluminium phosphate, magnestwm phosphate, calcium phosphate, calcium silicate and aluainium silicate.

The precipitated salt may be formed in a known way by reaction of suitable salt-forming reagents in the said suspension. Addition of a carbon dioxide containing fluid to an alkaline earth metal hydroxide in the said suspension is preferred to form an alkaline earth metal carbonate because of the availability, relative cheapness and ease of applicability S of these reagents and the neutral and fine nature of the product so formed.

The particulate material and fibres, eg. cellulose fibres GB95/002 04110/96

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present in de-ink reject sludge consists predominantly of "fines", in other words the material which, according to TAPPI Standard No. T 261 cm-90, will pass through a round hole of diameter 76pm. Generally, the particulate and fibrous material present in the sludge will contain at least 75% of, and usually will consist substantially completely of, particles and fibres that will pass through a round hole of diameter 76m.

Surprisingly, it has been found that the method according to the present invention can be used to obtain from a deinking plant waste which has a noticeable grey colour, a particulate product which is sufficiently light in colour to be useful for recycling for re-use, eg. in a paper making process.

Thus, surprisingly and beneficially the present invention allows useful material to be recovered from de-inking reject sludge without having to separate the ink from other material in the reject, and allows the cost of disposing of such sludge to be reduced or eliminated.

The method of forming a precipitate in an aqueous suspension to entrain fines therein is described in Applicant's EP 0604095. Use of the method to treat the effluent white water from a paper making process is described in Applicant's EP 658606 published after the priority date of the present Application. However, use of that method to treat S the dark ink-containing reject material from a de-inking plant is not disclosed or suggested in the said published specifications. Such method provides surprisingly, an example of a way of carrying out the present invention.

The precipitate product obtained by the method according to the present invention may be useful with or without further processing and with or without addition to other materials in S any of the various applications in which particulate inorganic e9 materials are known to be useful, eg. as compositions for adding as pigments, fillers or extenders for adding to paper, paper coatings, polymers, plastics, paints and the like.

GB95/002 04/10/96 Such product will include in addition to the precipitate material, eg. calcium carbonate, formed in the suspension entrained and aggregated particles and fibres contained in the suspension treated possibly together with precipitated material originally contained in solution in the water-based medium from which the suspension is formed. The entrained and aggregated particles will include ink particles as well as inorganic particulate materials employed as coating and/or fillers in the paper forming the original waste material, eg.

particles of one or more of kaolin, metakaolin, calcium carbonate, calcium sulphate, titanium dioxide, mica and talc.

The composition of the solid content of the product formed by the method according to the present invention may comprise from 5% to 95% by weight precipitate and from 95% to by weight particles and fibres entrained or aggregated into the precipitate.

As an example of re-use of the product of the method according to the present invention, a paper coating composition may be formed using the product by mixing an aqueous suspension of pigment material comprising the product optionally together with other pigments together with an adhesive. The other pigments may for example comprise one or more of kaolin, calcium carbonate (which may be ground or e precipitated), calcium sulphate, mica, titanium dioxide and talc. The adhesive may form from 4% to 20% by weight based on the total dry weight of pigment or pigments present. The adhesive may be one of the known paper coating adhesives Semployed in the art, eg. chosen from the group consisting of starches, proteinaceous adhesives such as casein and latices of, eg. styrene butadiene rubbers and acrylic polymers. The paper coating composition may also include a thickener, eg. in an amount of up to 2% by weight based upon the total dry weight of pigment or pigments present. The thickener may S- comprise one or more substances employed as thickeners in the prior art, eg. sodium carboxymethyl cellulose or synthetic acrylic thickeners.

GB95/002 04/10/96 The paper coating composition may be formed by mixing together an aqueous suspension of the product of the method according to the present invention, preferably also containing a dispersant, eg. a polycarboxylate such as polyacrylate, optionally with one or more further aqueous dispersed suspensions containing other pigments, with the adhesive and any other optional constituents eg. thickener, in a manner familiar to those skilled in the art.

Where the product of the method according to the present invention is to be used as a filler for material such as paper, plastics, paint, polymers and the like the amount of filler employed comprising the product with or without other filler material is the same as may be employed in the prior art in similar uses of filler material, eg. the filled material may comprise up to 40% by weight filler particles including the said product and from 100 to 60% by weight material to be filled.

The aqueous suspension in which the de-inking reject is treated in the method according to the present invention may comprise slurry or sludge obtained from a flotation process in a de-inking plant. For example, the aqueous suspension in which the insoluble salt is precipitated may comprise the froth product recovered from the microflotation cells which are used to treat the water separated from the pulp in various .oo stages of a process for preparing a useful sheet forming material from waste paper, and especially from printed waste paper.

Alternatively, the aqueous suspension in which the ~insoluble salt is precipitated may comprise the froth product from the main flotation stage of a plant for de-inking office waste paper, as this generally contains less ink residue than water paper from other sources. When the product comprising precipitate of insoluble salt and entrained fine particles is intended for recycling to a plant producing newsprint, the aqueous suspension which is treated in accordance with the invention may be the dilute suspension which is obtained as a GB95/002 04,/0/96 result of washing the dewatered pulp obtained from the underflow product of the main flotation stage.

The aqueous suspension constituting the slurry to be treated may generally contain between about 2% and 10% by weight of solid material. Such a dilute suspension of fine particles is normally difficult to separate into its liquid and solid components.

The product comprising the precipitate eg. alkaline earth metal carbonate and entrained fine particulate and fibrous material, which is produced by the method according to the present invention, where re-used in paper making, may for example be used to supplement the particulate filler which is added to cellulosic fibre material in a paper sheet-forming process.

Also, the water separated from the suspension containing the precipitate, eg. alkaline earth metal carbonate and entrained fine particulate material, may be used in an earlier stage of a waste paper pulping plant or in an sheet-forming mill.

Where the precipitate formed in the method according to the present invention comprises an alkaline earth metal carbonate, the precipitate may be formed by introducing into the reject slurry to be treated a source of alkaline earth o e metal ions and a source of carbonate ions. These will form e the desired precipitate of alkaline earth metal carbonate in situ which will entrain the fine particles and fibres in the slurry. The first reagent which is added is preferably S uniformly dispersed throughout the slurry to avoid local concentration gradients. When the first reagent is sparingly to soluble, as is the case with 6 OO GB95/002 04/10/96 ambient temperature, but it is preferably heated to a temperature in the range of from 30 to 70 0 C, and the suspension of the alkaline earth metal oxide in the water is preferably agitated vigorously for a time of up to 30 minutes to ensure that slaking is complete.

When the alkaline earth metal is calcium and the source of carbonate ions is a carbon dioxide-containing gas, the production of calcium carbonate in the scalenohedral form is favoured by maintaining the temperature of the mixture of used water and calcium hydroxide in the range of from 20 to 65 0 C. The carbon dioxide-containing gas is preferably 100% CO 2 although it may contain from 5% to 100% by volume.

of CO 2 and other suitable gas, eg. air or nitrogen.

The quantity of the source of alkaline earth metal ions and of the source of carbonate ions used is preferably such as to precipitate sufficient alkaline earth metal carbonate to give a weight ratio of alkaline earth metal carbonate to fine particulate material in the range from 10:90 to 90:10, and most preferably in the range 30:70 to 70:30. The suspension containing the precipitate of alkaline earth metal carbonate and entrained fine particulate material may be recycled directly in its relatively dilute form to 25 supplement the filler being used in a sheet forming o*e process. Alternatively, the suspension containing the precipitate may be dewatered by any conventional method, for example by sedimentation, by pressure e :filtration, or in a centrifuge.

30 The suspension of the precipitate of alkaline earth metal carbonate and entrained fine particles is found to be very much easier to dewater than the original suspension of the fine particulate material S-alone, because, when a cake of the precipitate is formed by filtration or by centrifuging, the packing of the particles is such that the cake is very much more

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permeable to water than is a cake formed from the solid component of the used water alone. Also, the precipitate, in many cases, is found to have advantageous light scattering properties which make it suitable for use as a filler in a paper- or boardmaking process. The precipitate may also find use as a filler, for example, in polymeric compositions such as carpet backing compositions.

The invention will now be illustrated, by way of example, by reference to the accompanying drawing and Examples. The drawing is a flow diagram of a de-inking plant for recovering re-usable cellulosic material from printed waste paper, modified in accordance with the present invention.

Printed waste paper, PWP, is pulped in a pulper 1 with water containing sodium hydroxide, sodium silicate and a dispersing agent. Most of the water used has been recycled to the pulper from a later stage in the process through a conduit 2, as will be explained below. The pulp prepared in the pulper is passed through a screening system 3 which removes at 4 large items of contamination such as staples, paper clips and pieces of grit, and also a substantial part of the low density contaminants such as particles of plastics materials, and agglomerates of sticky material derived from adhesives, sizing reagents and pitch. Recycled water from a later stage in the process is delivered through a conduit 5 to assist the passage of fibres and fine particles through the screens and the discharge to 30 waste of coarse materials retained on the screens.

A collector reagent is then added to the aqueous suspension which has passed through the screening system, and the suspension is subjected to froth flotation in one or more flotation cells 6. A substantial proportion of the ink particles in the size range from 20 to 200jm in the suspension are removed in

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the froth which overflows from the top of the cells at 7 and a product depleted in ink is withdrawn from the bottom of the cells and transferred to a dewatering stage 8. In this stage cloudy water containing fine organic and inorganic particles is separated from the pulp and transferred through a conduit 9 to a first microflotation stage 10. The thickened pulp from the dewptering stage 8 is diluted with recycled water supplied through a conduit 11 and is washed on fine screens 12. Washing reject passing through the screens is removed through a conduit 13. A further dose of a dispersing agent is added, if necessary, to the pulp which is retained on the screens 12, and the pulp then enters a dispersion stage 14 where it is subjected to intense mechanical agitation in which any remaining ink agglomerates are broken down to particles not larger than about 20yxm and are prevented from reagglomerating.

The dispersed suspension is then passed through a second screening stage 15 which removes any remaining coarse particles and agglomerates and discharges them through a conduit 17. The screens are supplied with recycled water through a conduit 16 to assist the separation process.

The aqueous suspension passing through the screens 25 is then subjected to a second dewatering stage 18.

Cloudy water containing fine organic and inorganic particles is withdrawn from this stage through a conduit 19 to a second microflotation stage 20. The dewatered pulp is washed on a further set of fine 30 screens 21 and the washing reject which passes through the screens is discharged through a conduit 22. The pulp which is retained on the screens 21 is discharged at 23. This pulp is substantially free of ink particles and is suitable for use as a source of cellulosic fibres in a sheet forming process.

The froth product from the flotation stage 7 and

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__1 -11the washing reject which passes through the screens 12 pass through conduits 7 and 13, respectively, to a dewatering stage 26, from which cloudy water is discharged through a conduit 28 to join the cloudy water flowing through conduit 9 to the microflotation stage 10. A suspension of the coarse particles and agglomerates which were retained on the screens flows through a conduit 17, together with the washing reject passing through screens 21 and flowing through conduit 22, to a dewatering stage 27, from which cloudy water is discharged through a conduit 29 to join the cloudy water flowing through conduit 19 to the microflotation stage 20. A thickened effluent material is discharged from the dewatering stages 26 and 27 at The cloudy water passing through conduits 9 and 28 to microflotation cell 10, and through conduits 19 and 29 to microflotation cell 20, is charged with compressed air which comes out of solution as the cloudy water enters the base of the microflotation cells in the form of very fine bubbles which pass up through the cells carrying with them most of the suspended particulate material. A flocculant, such as polyacrylamide, may be added to the cloudy water 25 entering the microflotation cells to cause the fine particles to clump together. Bentonite may also be added to adsorb and remove any sticky material present in the cloudy water. -Clarified water is discharged from the bottom of microflotation cell 10 through 30 conduit 24 to supply the pulping stage 1 and the first screening stage 3 through conduits 2 and respectively. Similarly, clarified water is discharged from the bottom of microflotation cell 20 to the screening stages 12 and 15 through conduits 11 and 16, respectively. The froth product overflowing from the top of microflotation cells 10 and 20 at 25, which -12product comprises an aqueous suspension containing from about 2% by weight to about 8% by weight of fine organic and inorganic particles, is treated, in accordance with the invention, with calcium hydroxide in mixing tank 31 and the treated suspension is carbonated with carbon dioxide-containing gas in a reaction vessel 32, as described in the following Examples Output product is extracted via outlet 32a, Example 1 The froth product from the microflotation cells and 20 of a de-inking plant producing waste paper pulp for use in making newsprint consisted of an aqueous suspension containing 6.74r by weight of dry solids.

A sample of the aqueous suspension was diluted with water to a dry solids content of 1.3% by weight.

The temperature of the sample was raised to 50°C and there was added to the sample sufficient of a suspension containing 148g of calcium hydroxide per litre to provide, after carbonation with a carbon dioxide-containing gas, a weight of calcium carbonate equal to the weight of fine dry solid material in the sample. In other words, there was added sufficient of the calcium hydroxide suspension to provide 14.8g of calcium hydroxide per litre of the sample. A gas 25 containing 20% by volume of carbon dioxide, the remainder being air, was then admitted into the mixture of the froth product and calcium hydroxide, the temperature of the mixture being maintained at 50 0 C, at "a rate sufficient to supply 0.048 moles of carbon 30 dioxide per minute per mole of calcium hydroxide.

The gas was passed through the mixture until the pH fell to 7.0 which corresponded to a time of about minutes. An aggregated crystalline precipitate was formed, and samples of the aqueous suspension of this product, which resulted from the carbonation of the mixture of the froth product and calcium hydroxide, and

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II- -13which contained 2.6% by weight of dry solids, were tested for filtration rate and, after filtration and drying of the dry solid material in the suspension, for the brightness of the dry solids. Samples of the froth product before treatment were tested in the same way.

The results obtained are set forth in Table 1 below: Table 1 Before After treatment treatment Mineral content by weight) 49.4 72.8 CaCO 3 content by weight) 11.4 53.3 Kaolin content by weight) 38.0 19.5 Brightness 41.6 66.2 Filtration rate 0.06 0.45 The brightness of the dry solids was determined by measuring the reflectance of a prepared surface of the dried solids to light of wavelength 457nm with a Carl Zeiss "ELREPHO" brightness meter and comparing the result with the reflectance of light of the same wavelength from an ISO standard brightness surface.

""The filtration rate was measured by the procedure too% which was described in Appendix 1 below.

Hand sheets of paper filled with the aggregated crystalline precipitate obtained as described above S: were prepared in the following way. 2 litres of a suspension of a thermomechanical pulp containing 3.56% by weight of dry pulp was diluted to 10 litres with filtered water and was then disintegrated for minutes in a turbine mixer, the impeller rotating at a speed of 1500rpm. At this stage the stock contained approximately 0.7% by weight of dry pulp and the Canadian Standard Freeness was 130. The volume of 35 stock was made up to 20 litres with filtered water and the consistency was checked by forming a paper sheet

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-14from a small sample by draining on a suitable wire screen and drying and weighing the sheet thus formed.

Water was added if necessary to reduce the consistency to 0.3% by weight of dry pulp.

There was then added to the paper making stock thus formed and stirred in by hand sufficient of an aqueous suspension of the aggregated crystalline precipitate to provide 4% and 8% by weight, respectively, of the total dry solid material in the paper making stock. This was followed by the addition of 0.02% by weight, based on the total weight of dry solid material in the stock, of a retention aid.

Hand sheets were prepared from the fillercontaining paper making stock according to the procedure laid down in TAPPI Standard No. T205 om-88, "Forming handsheets for physical tests of pulp". For each hand sheet a sample of the stock was poured into the sheet forming machine and surplus water was removed.

The brightness, or percentage reflectance to violet light of the hand sheets was measured by means of a DATACOLOR 2000 brightness meter ficted with a No.

8 filter (457nm wavelength).

"The opacity of each sample of paper was measured by means of the DATACOLOR 2000 brightness meter fitted with a No. 10 filter (a green filter embracing a broad spectrum of wavelengths). A measurement of the percentage of the incident light reflected was made with a stack of ten sheets of paper over the black 30 cavity of the brightness meter Of these ten sheets, the top five were from the sample of paper currently under test, and the remaining five were sheets from other samples which were used merely to .ensure that the stack was completely opaque. The ten 35 sheets were then replaced with the single sheet from the top of the stack of five test sample sheets over r I I- the black cavity and a further measurement of the percentage reflectance was made The percentage opacity was calculated from the formula: Percentage opacity 100.R/Roo The procedure was performed five times with each time a different sheet of paper on top of the stack, and the complete sequence of steps was then repeated to give a total of ten results from which the average value of the percentage opacity was determined.

The hand sheets from each batch were also tested for Ibursting strength by the test prescribed in TAPPI Standard No. T403 om- 85. The bursting strength is defined by the hydrostatic pressure in kilopascals required to produce rupture of the material when the pressure is increased at a controlled constant rate through a rubber diaphragm to a circular area of the paper 30.5mm in diameter. The area of the material under test is initially flat and held rigidly at the circumference but is free to bulge during the test.

Samples of each sheet were also weighed dry, the weight of the dry sample being used to determine the weight per unit area of the paper in grams per square metre.

The burst strengths were divided by the weight per unit area of the -paper to give a burst ratio.

25 As a comparison, the experiment described above was repeated, but using as the filler in the paper making composition 4% and respectively, by weight of a precipitated calcium carbonate filler having a particle size distribution such that the weight median 30 particle diameter was 8 As a further comparison, hand sheets were prepared from paper making stock which contained no filler and subjected to the same tests as are described above.

The results obtained are set forth in Table 2 below. For the hand sheets prepared from stock containing filler, the burst ratio was expressed as a i _1 -16percentage of the value obtained for the unfilled hand sheets.

Table 2 Filler Brightness Opacity Burst ratio of value for unfilled sheet Unfilled 59.6 90.8 100 Precipiated 4% 59.9 91.8 95.7 calcium carbonate 8% 59.8 91.2 86.9 Aggregated 4% 57.0 92.8 97.3 crystalline filler 8% 55.9 93.2 90.3 These results show that although the brightness values achieved when the aggregated crystalline material is used as the filler are not as good as those obtained with the proprietary filler, the aggregated crystalline material shows a better opacity and causes a smaller reduction in the strength of the paper than the proprietary filler.

o* Example 2 Samples were taken of the froth product from the microflotation cells of a different de-inking plant, and the experiment described in Example 1 was repeated.

The solids content of the froth product was found to be 6.8% by weight, and the solids content of the suspension of aggregated crystalline filler which was produced after dilution of the froth product to a dry solids content of 2.25% by weight of dry and S 40 carbonation with a carbon dioxide- containing gas as described in Example 1 was 4.5% by weight. The properties of the solids in the initial froth product and in the suspension of the aggregated crystalline 0 -17filler, and the filtration rates of the two suspensions, are set forth in Table 3 below: Table 3 Before treatment Mineral content by weight) 52.7 CaCO 3 content by weight) 12.3 Kaolin content by weight) 40.4 Brightness ISO) 51.0 Filtration rate 0.03 After treatment 74.7 54.3 20.4 69.2 0.26 The properties of hand sheets prepared and tested as described in Example 1 and containing the aggregated crystalline filler in accordance with the invention, the proprietary precipitated calcium carbonate, and no filler, respectively, are set forth in Table 4 below: Table 4 Filler Brightness Opacity Burst ratio of value for unfilled sheet) a a.

.i Unfilled Precipitated calcium 35 carbonate Aggregated crystalline filler 59.6 59.9 59.8 59.6 60.4 90.8 91.8 91.2 92.8 93.6 100 95.7 86.9 95.7 88.8 o u r Appendix 1 Filtration rate measurement method A small sample of the suspension of the mixed mineral produced was poured into a Buchner filter funnel provided with a piece of standard filter paper, the side arm of the filtrate flask being connected to -18the laboratory vacuum source. The filtrate was collected in a measuring cylinder inside the filtrate flask, and at intervals the volume of filtrate collected and the time which had elapsed since the start of filtration were recorded. The square of the volume collected was plotted graphically against the elapsed time, and a curve was obtained which had a large central straight line portion. The slope of this straight line portion was recorded in each case.

The relationship between the square of the volume of filtrate collected and the elapsed time is given by the Carmen-Kozeny equation:- 2 2.A 2

E

3 (y 1) T 5.v.S 2 (1 E) 2 .d 2 where: Q is the volume of filtrate collected; T is the elapsed filtration time; A is the area of the filter medium; P is the differential pressure across the filter medium; E is the fraction of voidage in the filter cake; v is the viscosity of the suspending medium; S is the specific surface area of the particulate phase; and d is the specific gravity of the particulate phase.

The slope Q 2 /T of the straight line portion of the graph plotted for each suspension gives a measure of the filtration rate in each case and, since A, P, v, S and d can be assumed to be constant under the conditions of the experiment, a standardised filtration rate P can be found to be given by: -19- F 0 2 .R F- O-^

T

where: 1 c d

S,

R-

WC

S, Sc where: We is the weight fraction of water in the cake; Sc is the weight fraction of solids in the cake; 5 W, is the weight fraction of water in the suspension; and S is the weight fraction of solids in the suspension.

Throughout the description and claims of the specification the word "comprise" and variations of the word, such as "comprising" and "comprises" is not intended to exclude other additives, components, integers or steps.

Claims

1. A method of treating reject from a plant for de-inking waste paper which reject comprises a mixture of ink particles, inorganic particles and fibres which includes the step of forming in an aqueous suspension or slurry comprising said reject a precipitate of a substantially white insoluble salt which entrains or aggregates ink particles, inorganic particles and fibres contained in said reject whereby the darkness of the reject is reduced by formation of the precipitate.

2. A method as in claim 1 and wherein the precipitate comprises calcium carbonate formed by reacting carbon dioxide with calcium hydroxide in the said suspension.

3. A method as in claim 1 or claim 2 and wherein the precipitate and entrained or aggregate material therein is separated for re-use as a particulate coating or filler material.

4. A method as in any one of the preceding claims and wherein the said 15 pioduct is separated from water which after separation is clearer than when originally treated and is recycled for re-use. A method as in any one of the preceding claims and wherein the said reject is a slurry or sludge produced from a flotation process of a waste paper de- °e inking plant.

S00 S 20

6, A method as in any one of the preceding claims and wherein the said 0 aqueous suspension or slurry contains between 2% and 10% by weight of solid material.

7. A product comprising a substantially white precipitate having entrained or aggregated material in the particles thereof which has been produced by the method as claimed in any one of the preceding claims,

8. A product as claimed in claim 7 and which contains from 5% to 95% by weight precipitated material and from 95% to 5% by weight of material entrained or aggregated therein. -21-

9. Use of a product as claimed in claim 7 or 8 as an inorganic particulate coating, filling or extending material.

A composition for paper making comprising cellulosic fibres coated or filled with material comprising the product claimed in claim 7 or claim 8.

11. A method according to claim 1 substantially as hereinbefore described with reference to any of the examples. DATED: 23 February 1998 PHILLIPS ORMONDE FITZPATRICK S Attorneys for: ECC INTERNATIONAL LIMITED *o e• ft R1I 010r, ABSTRACT A method of treating reject from a plant for de-inking waste paper which reject comprises a mixture of ink particles, inorganic particles and fibres includes the step of forming in an aqueous suspension or slurry comprising said reject a precipitate of a substantially white insoluble salt which entrains or aggregates ink particles, inorganic particles and fibres contained in said reject whereby the darkness of the reject is reduced by formation of the precipitate. The precipitate may comprise calcium carbonate formed by reacting carbon dioxide with calcium hydroxide in the said suspension. The precipitate and entrained or aggregate material therein may be separated for re-use as a particulate coating or filler material. The said product may be separated from water which after separation is clearer than when originally treated and is recycled for re-use. The said reject may be a slurry or sludge produced from a flotation process of a waste paper de- inking plant. *9 oSo. S 0/09 o* 04/10/96