TITLE: PROCEDURE FOR IMPROVING DEWATERABILITY OF BIOSOLIDS CAKE AND PRODUCTION OF HIGHLY DEWATERED BIOSOLIDS CAKE

FIELD OF THE INVENTION [001 ] The invention relates to the further processing of biosolids cake in wastewater processing systems.

BACKGROUND

[002] Recovery, processing, off-site transport and reuse/disposal of biosolids is one of the most expensive costs of waste-water treatment processes. Consequently, there is great interest in developing processes which reduce these costs.

[003] A widely used practice is to de-water the biosolids material, using filters, centrifuges and/or presses, so as to produce a biosolids cake typically having a solids content of 18-24%. In this, only rarely and at high expense is a cake with a solids content of 25% or higher produced. This cake form material, as a solid, may be stored, transported and used as a fertilizer, incinerated or landfilled. This biosolids cake may be converted to a pumpable liquid, having a solids content of 10% or higher, which reduces pathogens, and facilitates handling, transport and land application by injection. [004] There is a great need for methods which reduce the volume of biosolids cake requiring transport off-site for re-use or disposal.

[005] It is well known that the organic make-up of biosolids, whether liquid, solid, in between, a mixture, all or both, renders the material difficult to de-water. Chemical polymers are widely used to promote flocculation of bacterial cells and other particulates, which make up digester biosolids effluents. Flocculation facilitates settling, dewatering and concentration of effluent solids in the process from about 1 -3% (raw waste) up to about 18-24% solids in typical biosolids cake. Chemical polymer usage often represents an expensive component of biosolids handling from raw waste to cake form. The EPA's fact sheet on centrifuge thickening and dewatering indicates that polymer costs for biosolids residuals dewatering can be as much as $80 per dry ton solids.

[006] Biosolids digester effluents are generally difficult to de-water due to the presence of colloidal materials and extra-cellular polymeric substances. These have the capacity to bind and capture large numbers of water molecules, thus making dewatering challenging. These effluents also have a variable amount of these components. The variability itself results in variable de-watering characteristics, and, consequently, variable amounts and costs of the chemical polymers required to achieve a specific dewatered cake solids content and the processing facilities required for high volume production. [007] Further variability in biosolids content results from common external processing factors, including mechanical forces and chemicals, which can affect de-waterability by interfering with flocculation processes. Mechanical forces reduce the strengths of, or sizes of, floes and cause deterioration of biosolids dewaterability. [008] The chemicals used for flocculating cells and other biosolids components often are multi- positively charged polymers, which bind to the negative charges on cells and other biosolids particulates, thereby bridging these particulates as part of the flocculating and dewatering process.

[009] Positively charged ions, such as sodium, potassium, calcium or magnesium, can also bind to these negatively charged particulates, thereby reducing interaction between flocculating polymers, cells and particulates. Therefore, addition of alkalis to digesters, including alkalis in the form of hydroxides of sodium, potassium, calcium or magnesium, can have the effect of reducing dewaterability and/or increasing the amounts of the very polymers required for dewatering.

[0010] While each sodium or potassium atom has one positive charge (ie monovalent) to react with particulates, each calcium or magnesium atom has two positive charges (ie divalent) and can neutralize two negative charges of the particulates. The less costly calcium or magnesium form has a more deleterious effect on the polymer's desired particle flocculating function. The effects of divalent ions, such as calcium or magnesium, are more complex because they can potentially also use their two charges to interact with the negative charges on two cells or particles, thereby bridging them and promoting flocculation. This conflict introduces even more variability in the process. [001 1 ] Mechanical treatment can result in cell disintegration and cause a reduction in the particle sizes of solid particles, and an increased number of those particles. This can also cause a negative effect on de-waterability. Disintegration releases negatively charged polysaccharides and other biopolymers, which are poorly degraded during digestion and increase flocculating polymer demand for dewatering.

[0012] Colloidal materials and extra-cellular polymeric substances tend to increase viscosity of biosolids. Mechanical treatments, including shearing, have a negative effect on de-watering, even though shearing can also reduce the viscosity of biosolids. The relationship between biomaterials viscosity reduction and de- watering is complex. For clarity, Figure 1 sets out an example discussed in US Patent 6,808,636 where 18% biosolids cake (BSC) 1 is mixed with alkali 2 in a mixer 3 for thorough combining and cooking, as at 5, for defined times and temperatures and the material 6 is severely sheared as at 7 in a single process. At that point what is optimally produced is a pumpable liquid 9 containing more than 18% solids which itself can be readily transported and used as a liquid fertilizer, as at 10. Experiments have shown that this liquid 9 is not readily dewatered further despite its liquid characteristics as at 8 without use of polymer at costs similar to those referenced by EPA above.

[0013] In addition, if the processed material fed back to digesters has been treated in a manner which has a negative effect on its dewaterability (for example through greater release from cells of colloidal materials or extracellular polymeric substances or through cell particle size reductions/increased numbers of particles), the non-degraded portion of these materials which emerges in the digester effluent will have a negative effect on dewaterability. This in turn will 90 cause an increase in chemical polymer demand for dewatering in the digester. A disadvantage of strategies which rely predominantly on feeding pre-treated unseparated biosolids back to digesters to reduce overall volumes of biosolids produced is that it takes a substantial period of time and much effort to demonstrate the effectiveness of any approach to potential users of the

95 technology (typically 3-6 months or longer to set up, run, sample and analyses a pilot digestion process simulating the large scale digesters in the plant of the potential user). Even so, the effectiveness of feeding the pre-treated biosolids back will vary with varying compositions of the biosolids produced in a particular plant and with varying digestion conditions and parameters.

100 [0014] In addition to being a rich source of fertilizer nitrogen and potassium, biosolids is also a rich source of phosphorus. In certain cases, where organic materials are used as fertilizers, including animal manures and biosolids, soils may be over-enriched with phosphorus, undesirably increasing phosphorus levels in runoff water and ultimately in rivers and lakes. Hence, some biological wastewater

105 treatment processes are being designed to promote biological phosphate removal, processes which may require digester augmentation with other substrates and co- digestion feeds such as glycerol.

DEFINITIONS

[0015] Biosolids in this application is organic matter recycled from sewage, 110 especially for us in agriculture.

[0016] Biosolids Cake in this application is a solid pre- or post-digested de- watered sewage sludge.

[0017] Solid in this application refers to a body of material which is not seen to slump under the influence of gravity at ambient temperatures.

115 [0018] Testing in this application includes both testing per se and use of a previously tested or verified result.

[0019] Solids Content in this application includes biosolids and other solids taken together. [0020] Shearing in this application is mechanical shearing substantially 120 beyond the mere mixing together of ingredients to the point where biological solids components of the biosolids cake are broken down mechanically, such as by disrupting the structure of cellular components.

OBJECTS OF THE INVENTION

[0021 ] One objective in reducing volumes of biosolids cake is to alter the 125 properties of the biosolids to improve the dewatering processes, such that the solids content of the cake is substantially increased above the typical 18-24% values.

[0022] Another objective is to develop a combination process, involving:

(a) enhanced pre-treatment and dewatering of biosolids, to reduce cake 130 volumes for off-site transport, and,

(b) feeding back the supernatant or liquid fraction to digesters for breakdown of some of the biosolids components present in the separated liquid phase.

[0023] Another objective is to develop means of reducing biosolids volumes 135 for re-use or disposal without increasing (or substantially increasing) polymer costs.

[0024] In a still further object of the invention to avoid the lower viscosities provided by combined thermochemical and shearing methods.

[0025] Another object is to reduce costs and also to reduce undesirable 140 phosphorus content digester fee back using calcium which causes phosphate to form an insoluble precipitate of calcium phosphate and heating further accelerates and promotes this precipitation. The objective is to reduce the phosphorus content by greater than 90%.

THE INVENTION

145 [0026] The invention provides a process producing highly dewatered biosolids cake (HDBC) involving biosolids cake pre-treatment followed by dewatering. [0027] In one aspect of the invention produces a dewatered biosolids cake product having a solids content of 30%, 35%, or more, and a supernatant or liquid fraction.

150 [0028] In another aspect of the invention the combination of the pre- treatment and dewatering processes of the invention with feeding back the supernatant/aqueous fraction to digesters greatly reduces the overall volume of biosolids requiring off-site transport for reuse or disposal.

[0029] Another aspect of the invention provides reduction of the overall 155 volume of biosolids requiring off site disposal by 30% or more and 40-50% or more.

[0030] A further aspect of the invention combines pre-treatment parameters which have a minimal negative on the effectiveness of flocculating polymers and/or which may be carried out without polymer use at all or minimized.

[0031 ] In another aspect of the invention avoids mechanical pretreatments 160 which reduce biosolids particles size, increase the number of particles and have an adverse effect on dewatering.

[0032] Yet a further aspect of the invention is to use alkali as the pre- treatment chemical and especially calcium oxide or calcium hydroxide.

[0033] Therefore, a further aspect of the invention is to reduce the overall 165 amount of pre-treated biosolids being fed back to digesters.

[0034] It is still another object of the invention to provide a biosolids cake (BSC) or sludge which is pre-treated and separated, such that the separated supernatant or liquid fraction is more biodegradable, and that fraction is fed back to the digester to augment the digestion process. The non-degraded portion of 170 these materials which emerges in the digester effluent will have less of a negative or have a negligible effect on de-waterability than would be the case if the pre- treated unseparated material is fed back. This in turn will cause a smaller increase in chemical polymer demand for dewatering.

[0035] And in another aspect the invention provides a process where pre- 175 treating biosolids sludge (BSC) followed by centrifugation or other separation means, produces a supernatant or liquid fraction (ie the more soluble fraction), in which the organic fraction as a percentage of total supernatant dry weight is enriched, and provide a more biodegradable and more utilizable digester feed, with minimal extra particulate matter. Hence, the feedback process, using this 180 organically enriched supernatant feed, will have a minimal or negligible affect on dewaterability and on polymer demand.

[0036] A further aspect of the invention is to pretreat and dewater biosolids cake in a manner in which the supernatant or separated liquid fraction is enriched with organic components, which are generally more biodegradable, and in which 185 the separated solids fraction is enriched with non-degradable (inorganics) and other less degradable materials (insoluble organics).

[0037] A still further aspect of the invention provides a significant advantage by using a hybrid process where the predominant volume reduction step is centrifugation, or another solids-liquid separation step, of the biosolids which have 190 been pre-treated in a manner which substantially increases de-waterability. This pre-treatment and dewatering can be demonstrated to potential users in a couple of days. The supernatant or separated liquid fraction represents a small fraction of the overall solids content (about 3-10%) and does not inhibit the digesters.

[0038] Hence, a further aspect of the invention is the provision of a hybrid 195 treatment, including dewatering, with supernatant fed back to a digester for processing, where the dominant step in reducing biosolids volume is pre-treatment and dewatering of BSC (Biosolids Cake) which is much more easily demonstrated to prospective users than processes which predominantly rely on pretreatment and digestion, which require prolonged and costly pilot demonstrations.

200 [0039] The invention also provides a biosolids cake pre-treatment, which includes the step of adding a substantial amount of alkali, specifically, calcium oxide or calcium hydroxide, as well as including a heating step, to promote precipitation of any phosphates as insoluble calcium phosphate. When biosolids cake (BSC), pretreated in this manner are dewatered, by centrifugation or another

205 solids-liquid separation step, the insoluble calcium phosphate is be separated with the solids or cake fraction (HDBC) and the process results in production of a supernatant or liquid fraction having a low phosphorus content.

[0040] A further aspect of the invention is the promotion of precipitation of phosphates with divalent cations, such as calcium, during the biosolids 210 pretreatment step and to separate those precipitated phosphates with the centrifuged or otherwise separated solids fraction.

[0041 ] A yet further aspect of the invention is to prepare a supernatant or separated liquid fraction, enriched with organic components but which is depleted in phosphorus and to feed back that liquid fraction to digesters depleted in 215 phosphorus to prepare a co-substrate for bio-dephosphorylation processes.

[0042] A further aspect of the invention is to further reduce the volume of the highly dewatered biosolids cake (HDBC) fraction using a drying process and to produce a fertilizer component with or without the additional drying.

FURTHER STATEMENT OF INVENTION

[0043] A process for improving the de-waterability of solid biosolids cake having an initial biosolids content of greater than 10%, 15% or 18% comprising placing a quantity of the biosolids cake in a reactor, raising and holding the pH of the biosolids cake to 1 1 or higher by the intermixing of the biosolids cake with an 5 alkali, and raising and holding the temperature of the biosolids cake to 80 degrees Celsius for a time period, or higher, and testing the biosolids cake, so treated, in a de-watering device wherein a liquid fraction is separated from a solids-containing fraction, and wherein the biosolids cake is treated by the combination of high temperature and alkali for a period of time sufficient for the solids-containing 10 fraction, preferably a solid, to have a biosolids content greater than the initial biosolids content.

[0044] The invention also provides a process for separating biosolids cake having an initial biosolids content of greater than 10%, 15% or 18% into a liquid fraction and a highly de-watered solids-containing fraction wherein said testing includes sending the biosolids cake, so treated, to a de-watering device wherein a liquid fraction is separated from a solids-containing fraction.

[0045] The invention also provides a process further including preparing the liquid fraction to be fed and feeding it back into digesters (or anaerobic) digesters without the solids-containing fraction and/or drying the solids-containing fraction for use as a fertilizer. [0046] The invention also provides a process excluding mechanical shearing of the biosolids cake prior to said testing or separation of the liquid fraction.

[0047] The invention further also provides a process wherein the alkali is one or more of or a mixture of CaO, CaOH, lime in which the amount of alkali added is greater than one of 10g, 15g or 20g as calcium hydroxide [Ca(OH)2] per Kg of 10% biosolids in the biosolids cake or its equivalent and, optionally wherein the alkali is increased proportionately with increased biosolids concentrations of the biosolids cake.

[0048] The invention further also provides a process wherein the temperature and time period hold of body of biosolids cake is 80-99.9 degrees Celsius and 6-24 hours, respectively, and optionally above 100 degrees Celsius for shorter periods.

[0049] The invention provides a process wherein the solids-containing fraction is transported to a site for use as a fertilizer, re-hydrated to form a liquid and presented as a liquid fertilizer. PREFERRED EMBODIMENTS

[0050] Twenty to twenty-five per cent biosolids cake 21 and Alkali in the form of lime or Ca(OH)2 (preferably Cal85) in a finely divided state to a process reactor25, being a cooker, wherein the input materials are mixed but not violently sheared 23 and heated 24. Upon or during the completion of the heating cycle mixed and cooked product is moved as at 26 to a separator 27 preferably in the form of a centrifuge. Centrifugation separates a solid -containing cake 28, preferably at about 40% total solids from a liquid fraction 29. Liquid fraction 29 may be fed back into a digester 30 for further processing.

[0051 ] Solids-containing cake 28 may be further processed 31 as by drying, or transported to a site for re-hydration into a pumpable liquid, fertilizer.

EXAMPLES

Settling by Gravity Over Time

[0052] Reduced ability of solids to settle by gravity {settleability} is sometimes used as an indicator of poorer dewaterability. In preliminary tests, studies were carried out on the effects of heat, alkali, calcium ions and shearing on settleability of biosolids using % settlability of 2% biosolids in a cylinder after 21 h. Settleability was expressed as height of the supernatant fraction as % of total liquid material height. In the result shearing had the most negative effect on solids settling (Table 1 ). [0053] Where solids typically settled to a compact 25-40% of the cylinder

(settleability 60-75%), after shearing the solids settled only to 52-89% of the cylinder contents (settleability 11 -48%). While shearing had the most negative impact on settleability, increasing the hold temperature also had a negative effect on settleability but to a lesser extent than shearing. Alkali treatments had a slight negative effect on settleability. Addition of CaCL ₂ had a negligible effect on settleability.

CST and Dewaterabilitiy

[0054] Capillary suction time (CST) values are widely used to predict dewaterabilities of biosolids liquids, that is, the lower CST value indicates better dewaterability.

Thermal Incubation

[0055] A separate batch of biosolids cake was diluted with tap water to 6%, incubated for 90 min at the temperatures indicated. The thermally treated biosolids samples were diluted to 3% solids and divided into two samples, one of which was sheared for 3 min in a Ninja single serve homogenizer. Dewaterability properties of the unsheared and sheared samples were measured as Capillary Suction Time (CST) values in seconds (Table 2). The samples were stored refrigerated for further testing.

Dewaterability deteriorates with thermal treatment and with shearing [0056] The results confirm the observations in Table 1 : Dewaterability gradually deteriorates with increase in thermal treatment while shearing has a major negative impact on dewaterability, almost doubling the CST time.

[0057] All further CST dewaterability tests were determined at a solids concentration of 3% (the test concentration typically used in literature reports). Dewaterability improves with digestion.

[0058] The above thermally treated samples from Table 2 (+/- homogenization or shearing) were digested for 15 days at 37C and again tested for dewaterability (Table 3). The general pattern shows that digestion improves dewaterability. However, the trends after digestion were the same as with pre- digested samples, ie deteriorating dewaterability due to homogenization/shearing and with increase in pre-treatment temperature.

More Severe Pre-Treatment / Low Alkali / No shearing

[0059] A more severe pre-treatment, holding 3% biosolids for 21 h at 80C and 90C with and without a low level of alkali addition (no shearing homogenization) also demonstrated similar patterns (Table 4). Dewaterabilities after pre- treatment and after digestion were extremely poor.

55C pre-treatment

[0060] A 20h pre-treatment of 8% biosolids was carried out at temperatures in the range 70-55C, 20h (+ an untreated control) and observed some excellent pre- and post-digestion dewatering results were observed for the 55C pre- treatment (Table 5).

The Thermo-Chemical Pre-treatment Invention Increased hydroxide plus prolonged thermal treatment

[0061 ] When biosolids was treated with increasing levels of Ca(OH) ₂ (all 85 greater than 3.3g/Kg 10% biosolids tested in Table 4) and held for 1 .5, 6 and 24h at 55C the more prolonged holds at higher alkali treatments led to dramatic improvements in dewaterability (Table 6).

[0062] Whereas untreated 3% biosolids exhibited a CST dewatering value (higher is poorer) of 340, and higher values are observed after thermal treatment 90 alone, post digestion values of -100, and especially -50, reflect outstanding dewaterabilities. The properties of biosolids with CST values of -200-1000 are more gel like on a subsequent filter whereas the solids in products with values of 100 and 50 are more particulate/grainy on the CST filter pad and the water just runs away.

95 Further Increased hydroxide treatment plus prolonged and elevated temperature holds.

[0063] Similar tests were carried out with increasing Ca(OH) ₂ treatments and thermal holds of 5h and 22h at 90C and 75C (Table 7). Post-digestion CST values after 22h holds at 75C and 90C after a 9 day digestion (-100 and even 40, 50) show 100 greatly improved dewaterability. Within each sub-group (1 -4, 5-8, etc.) pre- digestion dewaterabilities (CSTs) show a pattern of improved dewatering in conjunction with the increase in concentration of Ca(OH) ₂ in the Ca(OH) ₂ range of 10-15g per Kg 10% biosolids.

[0064] When biosolids cake was treated with increasing concentrations of

105 Ca(OH) ₂ in the range 12.5-20g/Kg 10% biosolids and held at 90C/20h (Table 8) biosolids dewaterability (no digestion) was shown to improve as a function of increasing Ca(OH) ₂ concentration. With these treatments, viscosities of the product (starting with 10% biosolids) reduced as a function of increasing Ca(OH) ₂ concentration. A single homogenization shearing test was carried out on the most 110 dewaterable sample (no 4). Dewaterability was poorer after homogenization.

Dewatering by Centrifuge [0065] Dewatering characteristics of biosolids cake, prepared using selected pre-treatment conditions were also tested using a bench centrifuge (15min., 6000xg). The tests (Table 9) using previous pre-treatment conditions show that

115 temperature holds of 20% biosolids 75-95C for 22h with 30-40g Ca(OH)2/Kg biosolids produced good dewatering with resulting pellet (solid fraction) solids contents of 25-26%. Lower alkali dose rates and inclusion of a homogenization step resulted in poor or no centrifugal separation, that is, very poor dewaterability. Best dewatera bili ties were observed in samples where pre-treatments of 20%

120 biosolids produced liquids with viscosity of <4000cps and preferably less than 2000cps. Combining homogenization (carried out after thermal) with this thermal alkaline treatment further reduced viscosities of 20% biosolids pre-treatment 95C, 22h, from 1770cps to 71 cps at a dose rate of 40g Ca(OH)2 per Kg 20% biosolids but those lead to a deterioration in biosolids dewatering properties. (714cps is similar

125 to viscosity treatment at 160C for 60min of 20-23% cake; and would correspond to 400-500cps at 15% biosolids).

Thermal Pre-treatment of 24% Biosolids Cake - Thermal Hydrolysis plus Alkali

[0066] The thermal pre-treatment was also carried out on 24% biosolids at 130 the typical high temperature for thermal hydrolysis (160C) for 60 minutes, with and without alkali. Following the pre-treatment, samples were cooled and centrifuged at 6000g, 15 min. The results are presented in Table 10. No separation occurred in the no alkali, 160C thermal treatment whereas a clear separation was observed in the thermal alkali treated sample and solids content in the solid 135 fraction pellet was 38%.

Thermal Pre-treament plus hot 95C certrifugation

[0067] Improved dewatering was observed when the 95C/22h (40g Ca(OH) ₂ /Kg 20%BS) treated material was preheated to 95C prior to centrifugation. In the experiment in Table 1 1 , it is shown that centrifuging hot material increased 140 the solids content of the solids fraction pellet (cake) to 34.3%. It should be noted that the hot material quickly cools down during this bench batch centrifugation. Even better dewatering than this is expected to be achieved through better maintenance of hot material temperature during centrifugation.

[0068] The negative effects of homogenization and the positive effects of centrifuging pre-heated material were confirmed in the tests summarized in Table 12 where solids content in the solids fraction pellet from hot pre-treated product was 36.5%.

Thermal Pre-treament at 121 C plus hot certrifugation

[0069] The thermal pretreatment was also carried out on 24% biosolids at typical autoclaving temperatures, 121 C for 75min., with and without alkali. Following the pre-treatment samples were cooled to about 90C and centrifuged hot at 6000g, 15 min. The results are presented in Table 13. Again, no separation occurred in the no alkali, thermal treatment whereas a clear separation was observed in the thermal alkali treated sample and the solids content in the solids fraction pellet was 37%.

Moist Surface Upon Separation

[0070] In these bench scale batch centrifugations when the supernatant is poured from the centrifuge tube it is noted that the pellet surface remains quite moist. In Table 14, following pouring off the supernatant the tube was cut to divide the solids fraction pellet into two portions, the top half and bottom half. The solids contents of the total solid fraction pellet, top half of pellet and bottom half of pellet were 37.7%, 28.8% (Lower solids concentration top half) and 45.3% (higher-solids-concentration-bottom-half), respectively. The solids content in the supernatant was 7.5%. Volatile (organic) solids content in the supernatant was 76.7% and 44.6% in the pellet. In the top and bottom half of the pellet volatile solids contents were 54.5% and 39.2%, respectively. In other tests centrifuged pellets having solids contents of >40% have been prepared.

Results

[0071 ] The results indicate the above biosolids cake ThermoChemical Pretreatment produces a dewatered cake having -40% solids in the solids fraction. The combined effect of dewatering to -40% solids and feeding back the organically rich supernatant (liquid fraction) to digesters allows for a reduction of 50% or more in biosolids requiring off site disposal.

[0072] Centrifugation conditions can be manipulated to capture as cake the 175 higher-solids-concentration-bottom-half solids fraction described above providing further reductions in biosolids needing to go off site.

[0073] Feeding back dewatered biosolids (untreated or treated) for co- digestion is counterproductive as it will have the effect of increasing the solids load in the digester.

180 [0074] In contrast, feeding pure organic carbon sources such as glycerol to digesters for co-digestion provides no change in dewaterability. The feedback of a rich organic supernatant rather than pretreated unseparated liquid biosolids is beneficial in minimizing any increase in solids loading and the flocculent (polymer) use.

185

Table 1. Effect of Biosolids Pre-treatment on Settleability

Ca(OH) ₂ Holdi Temperature % Settleability after

g/L per 10% BS (90min)

1. Heat treatment 2. Heat treatment 3. Heat treatment (pH after + addition of + addition of treatment) CaCL2 CaCL2

+ shearing

0 Room 75.8 (8.0) 73.8 53.7

3.3 73.8 (8.3) 73.8 52.4

10 73.8 (9.2) 73.8 547.5

0 60C 76.9 (8.0) 78.6 53.8

3.3 75.0 (8.3) 76.8

6.6 71.7 (8.7) 71.8

10 69.7 (9.0) 71.4 50.0

0 70C 71.0 (8.0) 72.5 51.0

3.3 70.3 (8.3) 70.7

606 67.2 (8.7) 69.3

10 68.8 (9.2) 68.8 51.3

0 80C 69.7 (8.0) 71.4 47.6

303 64.1 (8.4) 65.0

606 65.6 (8.7) 67.5

10 64.0 (9.2) 67.9 47.6

0 90C 59.0 (8.2 64.2 11.0

3.3 59.4 (8.4) 61

10 67.0 (9.4) 66 29.5

*% Settleability after 21h = (height of supernatant/total height of liquid)xl00

Different amounts of calcium hydroxide were mixed into biosolids (2%w/w). Each mixture was incubated at room temperature, 60C, 70C, 80C, 90C for 90minutes. Each treated mixture was cooled to room temperature and added to cylinders [4.4cm (internal diameter) x 25cm (height)] . The cylinders were held at room temperature for 21h to allow solids to settle out. Calcium chloride was then added to each cylinder at a rate equivalent to 2% of dry biosolids content. The contents of each cylinder was remixed and allowed stand again at room temperature for 21h after which settleability was again measured. Finally the contents of selected cylinders were violently mechanically sheared in a Ninja Homogenizer for 3 minutes. The sheared mixtures were placed back in the cylinders and allowed to stand again at room temperature for 21h after which settleability was again measured.

Table 2. Effects of Biosolids Thermal Pretreatment on CSTs Incubation Temperature C Dewaterability (CST)

(90min)

No Homogenisation Homogenisation shear (Ninja single serve - 3 min)

Room 343 597

60 352 690

70 429 698

80 488 899

90 617 1232

Avg 446 Avg 823

Table 3 Effect of pretreatment temp and homogenization on dewaterability of biosolids(CST)

Thermally treated 6% BS samples from Table 2 were diluted to 3%. 180g of the diluted samples was placed in an anaerobic digester together with 40g of a 3% inoculum and digested at 37C.

Hold *Homo CST Digestion Time CST after Temp g 3 Min (3%) (in days) digestion

90min (Ninja) T5 T10 T15 T16 T20

T

24C No 343 468 632 721 260 227

24C Yes 597 416 605 688 387 368

60C No 352 420 675 868 352 240

60C Yes 690 396 652 755 475 441

70C No 429 434 701 795 387 355

70C Yes 698 Net gas mL/reactor 414 705 811 527 506

80C No 488 492 769 892 447 399

80C Yes 899 473 780 879 486 577

90C No 617 spill

90C Yes 1232 474 821 911 915 707

Avg No Shear 446 *361 *305

Avg with Shear 823 *469 *473

*excl 90's because of spill

iolently sheared after thermal hold

Table 4. Effect of thermal +/- alkali pretreatment and digestion on CST of 3%BS

(Digestion conditions as in Table 3)

Table 5. Effect of temperature pretreatment of 8% BS and digestion on dewaterability (CST)

(Digestion conditions as in Table 3)

Table 6. Effect of pretreatment temp +/- alkali of 3% biosolids on digestion and CST

(Digestion conditions as in Table 3)

Table 7. Effect of pretreatment temp +/- alkali and digestion on CST of 3%BS

(Digestion 180g 3%BS, 35g Inoculum) Untreated CST3% 348

Table 8. Effect of Thermal (90C/20h) /Alkali treatment of 10% BS on CST and Viscosity Untreated biosolids had a CST (at 3% BS) of 348

Number Ca(0H)2 pH after CST (Sec) Viscosity CST3% CST3%

g/L10%BS treatment 10% BS After After

(cps) 3 days Homog/Shear

10% for 90sec after 3d

1 12.5 9.4 1353 1752

2 15 9.6 633 1392

3 17.5 10.1 302 828

4 20.0 10.7 150 336 250 404

Table 9. Effect of pretreatment temperature, alkali dose and homogenization of 20% biosolids on viscosity, CST value and centrifugation

Untreated biosolids CST at 3% solids: 348

Table 11. Effect of temperature of thermal + alkali pretreated BS on centrifugation effectiveness

Pre-Treat conditions: 20% solids. Untreated CST3% 348 Hold Ca(OH)2 Vi sco sit Solids CST 3% Centrifuged 6000g 15min

Temp/ti g/L per y Conte

me 10% BS 20%BS nt %

Distribution Solids Content

% %

Supe Pelle Supe Pelle r t r t

95C 20 1770 22.0 174 No 36.7 63.3 7.7 31.2 22h Preheat

*Prehea 41.0 59.0 6.9 34.3 t

*Preheat: Metal casing + Tube + contents preheatec 95C/15min

Table 14. Characterization of pellet (cake) from thermal + alkali pretreated BS, preheated to 95C/15min before centrifugation

Pre-Treat conditions: Prepared 22% Biosolids with 40g Ca(OH)2 per Kg 20% Cake. Crock Potted unmixed on low 98C for 20h. Re lenished eva orated water. Final dr wt 22.80%.

Preheat: Metal casing + Tube + contents 95C/15min

[0075] Accordingly, it will be understood that reasonable variations and modifications of the invention disclosed herein above are possible, whereby the specific illustrative examples set out herein are not to be construed as restrictive 240 to the broad features of the present invention.

LIST OF ELEMENTS

245 1 18% biosolids cake

2 alkali

3 mix/cooker

6 resulting material

7 severely sheared

250 8 no further watering

9 liquid

10 liquid fertilizer

21 biosolids cake

22 alkali, finely divided

255 23 mixed

24 heated and held reactor

product moved to dewatering separator-dewatering

solids-containing cake

liquid fraction

digester

dewatered BSC further processed