SYSTEM FOR WASHING BIOLOGICAL WASTE TO RECOVER SAME AS SOLID BIOFUEL

Abstract

This development describes a system, a method and specific products for washing biological waste, preferably animal manure, particularly cattle manure, particularly biological waste with high silica content and agro-industrial and forestry waste products to obtain a purified lignocellulosic product with a high calorific value that, when burned, releases low concentrations of harmful gases and does not generate or generates little vitrification inside.

Claims

1. A continuous low energy consumption method for obtaining a solid fuel comprising ligno-cellulose based on biological material from cattle manure, wherein this biological material is fed to a washing system (I), where after this biological material passes through the washing system (I), the organic material is transported through passage (16) where it is pressed or centrifuged (O), eliminating excess water from the material, which is subsequently taken through passage (18) to a dryer (P), which is fed with a current of hot air generated by a boiler (Q) through passage (21), where then through passage (19) the material is sieved and/or passed through dry so vibration magnetism (S), where this powder-like organic material can then be pelletised (T) through passage (20) and/or formed into briquettes (T) and/or be kept as powder without pelletising, CHARACTERISED in that the washing system (I) includes the following consecutive steps: i) impulsion through a slurry pump (a); ii) initial granulometric filtering; iii) dosage; iv) centripetal or centrifugal movement with water turbulence and optional injection of ozone; inside the washing and humidification tank (e); v) cavitation and impingement; vi) final granulometric filtering; vii) dehydration by screw hammer mill (j).

2. A continuous low energy consumption method for obtaining a solid fuel comprising ligno-cellulose based on biological material from cattle manure according to claim 1, CHARACTERISED in that the initial granulometric filtration (ii) and the final granulometric filtration (vi) steps filter a solid with a size greater than the range between 0.841 to 2 mm for the first filtration, and a solid with a size greater than the range between 0.25 to 2 mm for the second filtration, where optionally in both steps (ii) and (iv) the filtering is accompanied with vibration.

3. A continuous low energy consumption method for obtaining a solid fuel comprising ligno-cellulose based on biological material from cattle manure according to claim 1, CHARACTERISED in that the cavitation and impingement step (v), is a passive or very low energy consumption step based only on the consumption of the cavitator pump (g1), achieving in milliseconds a pressure drop of over 50% with respect to the inlet pressure in this step, where cavitation is produced aerobically and/or with ozone, generating gaseous products that are extracted and channeled for later use, where cavitation also optimises the processes of internal and external cleaning and sanitization of the fibre, where in addition the liquid that will pass through cavitation has a diluted fibre content in the range of 0.5% to 5%, where in addition the flow impingement is preferred between flows in opposite directions or against a plate, with a distance between flows or between the flow and the plate of between 1 cm to 200 cm, following the relationship that the smaller the distance the greater the shredding of the fibre.

4. A continuous low energy consumption method for obtaining a solid fuel comprising ligno-cellulose based on biological material from cattle manure according to claim 1, CHARACTERISED in that the dehydration step (vii) compresses the fibre between the first extruder mill element and breaks it up with the hammer mill element, generating percentages of less than 30% moisture in dry weight of the fibre.

5. A washing system as described in clause 1, CHARACTERISED in that it comprises a slurry pump (a) that moves the material from the slurry pit (A) through a solids and liquids separator (C), and then deposits the wet solid on an initial screen, sieve or rotary filter device (b), where the solid mainly filters the liquids and then falls into a feed screw (c) that deposits the contents in the dosing device (d), where the quantities of fibre to be hydrated are sectioned in a washing and humidification tank (e), where this solid is agitated with water and optionally ozone is applied from the attached ozone preparation tank (o) and then extracted to the cavitation and impingement tank (g), where the jets are cavitated and impinged against each other or against a plate to internally and externally shred the fibre, where the wet solid is then sieved on a final screen, sieve or rotary filter (h) and finally the same solid is extruded and broken up with the hammer mill screw device (j), to be finally delivered to the final drying steps.

6. A washing system as described in clause 5, CHARACTERISED in that the initial (b) and final (h) screen, sieve or rotary filter type devices comprise an initial filter mesh size between 2 mm to 0.841 mm and a final filter mesh size between 2 mm to 0.841 mm, in addition there may be one or more filters in series or in parallel, and in addition there may be vibration.

7. A washing system as described in clause 5, CHARACTERISED in that the washing and humidification tank (e) comprises a tank with a capacity of between 5 to 100 m.sup.3, with an inlet for the washing water (e1), which can go above or below the tank, and through this inlet, the optional injection of ozone (O.sub.3), with a second entry point for the solids (e2) to be treated, where in the centre of the tank there is a tubular paddle agitating apparatus (e3), where also on the other hand, the washing water from the first injection (e1) generates a stream that carries the solids, separating it in combination with the effect of the previously mentioned centripetal movement, where optionally the contents of said washing and humidification tank (e) can simply be centrifugally agitated from the centre by paddles with the respective washing water from the first inlet (e1) generating a stream that entrains and separates the solids, where furthermore the excess liquid in said washing and humidification tank (e) is expelled through the level transfer outlet (e4) in the upper part of the washing and humidification tank (e), transferring the contents back to the slurry pit or tank (A), where the washing and humidification tank (e) also performs the function of homogenising and degassing the excess ozone (O.sub.3).

8. A washing system as described in clause 5, CHARACTERISED in that the transfer of solids from the washing and humidification tank (e) is by means of cavitator pumps (g1) to the cavitation and impingement basin (g) comprising the cavitation and impingement duct(s) (g2), which in turn comprise two main interconnected structures, the cavitation and laminar flow duct (g2a) and the impingement duct (g2b), wherein the cavitation and laminar flow duct (g2a) comprises a tubular shaped structure with tapered internal and external diameters, wherein internally the cavitation ducts (g2) comprise three sections, arranged from where the waste flow enters to where it exits, starting with the diameter of the inlet duct (g2ad) in the first nozzle section (g2aa) where the internal diameter of the cavitation duct (g2) is tapered with a nozzle angle between 15° and 35°, where this tapering of the internal diameter (g2ae) of the cavitation duct (g2), goes from a slight reduction of the inlet internal diameter of the cavitation duct (g2) to ⅕ of the internal diameter, after which comes the second flow load section (g2ab), which maintains a constant internal diameter in relation to the tapering of the internal diameter of the previous section, then comes the third and last section of the diffuser (g2ac) where the internal diameter of the cavitation duct (g2) widens again at an angle between 5° and 10° until it reaches the same inlet diameter (g2ad) of the cavitation duct (g2), this is where the cavitation effect is generated as the flow passes the edge of the angle formed when the diameter of the duct expands, generating a sudden pressure drop with the production of micro bubbles in the fluid and its coalescence, where continuing in the direction of the flow, a second element called a impingement duct (g2b) is connected comprising three sections, where the first section maintains the same internal diameter of the inlet (g2ae) to the cavitation duct (g2) and is called a separation section (g2ba), where it is given a physical space for the waste component elements to separate, and then the outlet reduction section (g2bb) is connected, where the inlet diameter (g2ad) is reduced to a larger diameter (g2bd) with respect to the reduction diameter (g2ae) of the flow load section (g2ab), in the range of 45% to slightly less than the internal diameter of the cavitation duct (g2), where the angle of the reduction in this section is in the range of 25° to 35°, then comes the outlet section (g2bc), which guides the outlet jet into the cavitation and impingement basin (g) where two outlet jets are then impinged against each other, or one outlet jet against one of the basin walls, or against a foil or baffle, where the direction of impingement between jets is preferably head on, although it can be angled if there are more than two jets, at a distance between 1 cm to 200 cm, where the capacity to shred the fibres of the jets is indirectly related to the distances between the impingement ducts (g2b), where to improve the frontal impingement of two jets the steering and impingement tube (g2h) is arranged, which consists of a tube with the same diameter as the impingement duct outlet (g2b) but with two lateral perforations (g2f) and a lower central perforation (g2g) that fulfil the objective of channeling the impingement explosion and the fall of the solid by product outlet (g3a), where also for the elimination of these volatile contaminants, the cavitation and impingement tank (g) includes in its upper part a gas outlet duct (g3d) that so channels and bubbles the gases into the biological material concentrate and inert impurities tank (G), finally, the cavitation and impingement tank (g) has a handle (g3b) for maintenance of the cavitation ducts and a viewer (g3c) to check the operation of the device.

9. A washing system as described in clause 5, CHARACTERISED in that the is hammer mill screw device (j) is a compact device operating with two elements, firstly an extruder mill element and secondly a hammer mill element, wherein the first extruder mill element comprises the following interrelated elements, an inlet hopper (j6) that channels the solids through the screw shaft (j1) which moves the solids against the tightening system (j8), wherein the screw shaft (j1) in turn comprises a continuous helix pipe (j1a) with an angle of rotation ranging from 15° to 50°, further comprising two pipe end bushings (j1b), with an inner pipe reinforcement (j1c), all mounted on a shaft (j1d), with a shaft end bushing (j1e), wherein the screw shaft (j1) is also supported in the extruder screw element of the hammer mill screw device (j) by a rear support (j2) and mounted on two tapered circular bearings (j3) to maintain the movement of the screw shaft (j1), these bearings being held to prevent their run-out following the line of the shaft, by clamping sleeves (j5), in parallel an o-ring (j4) separates these bearings (j3) from the material entering the inlet hopper (j6), following the screw shaft (j1), before reaching the clamping system (j8), it passes through a screening device (j7), comprising a circular screen (j7a) with between 80 and 1000 platens, with a mesh size between 0.05 and 3 mm, supported on a screen support (j7c) and enclosed in the screen casing (j7b), which channels the water extracted in the squeezing through the drain (j7f) to be recirculated, retaining the solids on the surface wherein the screen device (j7) is easily removable by means of the screen handle (j7e) and the removal of the device cover (j7d) for cleaning, wherein the tightening system (j8) is bounded by the upper (j22), upper side (j23) and lower side (j20) covers which support the accumulation of solid material shredded by means of the blades (j8e) which are fastened to the blade holder (j8a), which in turn is stabilised on the horizontal axis by the spring (j8c), which in turn exerts pressure against the direction of the material by the screw shaft (j1), where to be attached to the extruder mill element of the hammer mill screw device (j), it is mounted through a lever holder (j8b) which holds the lever (j8d), which holds the tightening system (j8) to the entire device in case the blades (j8e) need to be replaced, wherein the tightening system (j8) compresses and shreds the solids and these accumulate partly on the screw shaft (j1), releasing liquid into the sieve device (j7), however, most of the solids fall by pressure and gravity into the grinding assembly (j14) or a traditional hammer mill corresponding to the second element of the hammer mill screw device (j), wherein this grinding assembly (j14) comprises a support housing (j14c) and a circular outlet of solid material (j14b), wherein internally it comprises a set of symmetrical cross-shaped grinding or shredding blades (j14a) mounted on a tube (j14i), which rotates about a square grinding shaft (j14h), wherein for this rotation, the grinding shaft (j14h) is positioned between two square-based bearings (j14d) at each end of the tube outside the housing, where the blades are rotated by the energy delivered by the rotation of the pinion (j14f) and by the pressure exerted by the solid as it is forced out by the restriction generated by a grate (j14g) with a mesh size slightly greater than the thickness of the blade, where, in order for the grinding assembly to be in position and for its shaft to freely rotate, it also contains a grinding assembly support bearing (j14e), which is mounted on the grinding assembly support (j17), on the screw shaft (j1), after the tightening system (j8), comes the bearing (j9) and the main support (j16) which holds most of the hammer mill screw device (j), then comes the pinion area, delimited by the top cover (j19) and the side covers (j21), this area protects the large (j10) and small (j11) pinion set mounted on the shaft (j1d), where the large pinion (j10) provides the mechanical power to the grinding assembly (j14), after this comes the gear motor (j12) which delivers power to the whole hammer mill screw device (j), where this motor is directly associated by means of a standard motor shaft (j13) to the shaft Old) to deliver the rotation to the whole device, where finally, the motor is supported on the motor base (j18) and is positioned by the motor support (j15).

10. A solid fuel product based on biological material according to claim 1, CHARACTERISED in that it comprises: ligno-cellulose, with an average particle size between 0.595-0.297, total nitrogen as a percentage of dry weight between 0%-0.5% w/w, total humidity in dry weight of 1%-10% w/w, superior calorific value of 4200-5700 kcal/kg under standard UNE-EN 14918:2011, lower calorific value of 4000-5300 kcal/kg under standard UNE-EN 14918:2011, ash in dry weight of 0%-3% w/w, and sulphur in dry weight of 0%-0.2% w/w.

11. Solid combustible product based on biological material, according to claim 10, CHARACTERISED in that it can be compacted in different ways, including, without limitation, briquettes, pellets, or another high-density mould.

Description

DESCRIPTION OF THE FIGURES

[0126] FIG. 1:

[0127] FIG. 1 shows a block diagram of the state of the art of application PCT/CL2017/00009 for the treatment of slurry to obtain lignocellulose as a raw material and/or fuel and other chemical components. Operations are shown in blocks, flow lines or streams are represented with arrows which indicate flow direction and are also represented by numbers.

[0128] FIG. 2:

[0129] This figure describes a diagram with the steps of the present development and how they are partly related to steps of the previous state of the art.

[0130] FIG. 3:

[0131] This figure presents only a diagram of the component elements of the washing system (I). Where they are indicated according to their numbering: [0132] A: slurry pit [0133] b: initial screen, sieve or rotary filter type device [0134] c: feeder screw device [0135] d: dosing device [0136] e: washing and humidification tank [0137] e1: inlet for washing water [0138] e2: entry point for the solid [0139] e3: tubular paddle agitator [0140] e4: level transfer output [0141] G: biological material concentrate and inert impurities tank [0142] g: cavitation and impingement tanks [0143] g1: cavitator pumps [0144] g2: cavitation ducts [0145] g3d: gas outlet duct [0146] h: final screen, sieve or rotary filter type device [0147] j: hammer mill screw device [0148] p: ozone-generating machines [0149] o: attached tank for ozone preparation [0150] O: press or centrifuge

[0151] FIG. 4:

[0152] This figure shows the cavitation and impingement tank (g), its cavitation duct (g2a), the relationship of its internal components, between the cavitation and laminar flow duct (g2a) and the impingement duct (g2b) and its different parts. The numbers indicate: [0153] g: cavitation and impingement tank [0154] g2: cavitation ducts [0155] g2a: cavitation and laminar flow duct [0156] g2aa: first nozzle section [0157] g2ab: flow load section [0158] g2ac: diffuser section [0159] g2ad: inlet duct diameter [0160] g2ae: internal diameter reduction [0161] g2b: impingement duct [0162] g2ba: separation section [0163] g2bb: output reduction section [0164] g2bc: output section [0165] g2bd: top diameter [0166] g2f: side perforations [0167] g2g: central bottom perforation [0168] g2h: steering and impingement tube [0169] g3a: product output [0170] g3b: handle [0171] g3c: viewer [0172] g3d: gas outlet duct

[0173] FIG. 5:

[0174] This figure shows the angle of collision of the jets coming out of two impingement ducts (g2b) and how they behave when they leave the device.

[0175] FIG. 6:

[0176] This figure shows the hammer mill screw device (j), showing all its parts and pieces, where the numbers indicate: [0177] j1: screw shaft [0178] j1a: pipe with helix [0179] j1b: pipe end bushings [0180] j1c: internal pipe reinforcement [0181] j1d: shaft [0182] j1e: shaft end bushing [0183] j2: rear support [0184] j3: circular bearings [0185] j4: o-ring [0186] j5: clamping sleeves [0187] j6: input hopper [0188] j7: sieve device [0189] j7a: circular sieve [0190] j7b: sieve casing [0191] j7c: sieve support [0192] j7d: device cover [0193] j7e: sieve handle [0194] j7f: drain [0195] j8: tightening system [0196] j8a: blade holder [0197] j8b: lever holder [0198] j8c: spring [0199] j8d: lever [0200] j8e: blades [0201] j9: bearing [0202] j10: large pinion [0203] j11: small pinion [0204] j12: reducer motor [0205] j13: standard motor shaft [0206] j14: grinding assembly [0207] j14a: symmetrical cross-shaped grinding blades [0208] j14b: circular output for solid material [0209] j14c: support box [0210] j14d: square base bearings [0211] j14e: grinding assembly support bearing [0212] j14f: grinding assembly pinion [0213] j14g: grid [0214] j14h: square grinding shaft [0215] j14i: tube [0216] j15: motor support [0217] j16: main support [0218] j17: grinding assembly support [0219] j18: motor base [0220] j19: upper cover of the pinion area [0221] j20: lower side cover of the tightening system [0222] j21: side covers of the pinion area [0223] j22: upper cover of the tightening system [0224] j23: upper side cover of the tightening system

EXAMPLE OF APPLICATION

[0225] This example was developed in the slurry pits of the Las Garzas agricultural laboratory.

[0226] On Aug. 17, 2020, 5450 kg of mainly bovine slurry were used and the procedure of the present development was applied. The cleaning water used comes from a well in the area, with water with a high content of dissolved salts.

[0227] Slurry and manure samples were taken initially, delivering the following summary of analytical results, as shown in Table II:

TABLE-US-00002 TABLE II Unit of Parameter measured measurement Slurry pit Manure Higher Calorific Power (kcal/kg) 3,376 3,571 Lower Calorific Power (kcal/kg) 3,107 3,277 Lignin (%) 2.4 24.7 Cellulose and hemicellulose (%) 4.5 45 Particle size (mm) NS 10-0.595 (67% of particles) Total Humidity (%) 89.21 9.13 Ash (%) 18.5 26.57 RAW MATERIAL COMPOUNDS Sulphur (%) 0.3563 0.3598 Carbon (%) 40.76 42.98 Hydrogen (%) 5,242 5,687 Nitrogen (%) 1.797 2.908 Oxygen (%) NS NS Mn (Manganese) (ppm) 130.43 166.45 As (Arsenic) (ppm) <0.01 <0.01 Pb (Lead) (ppm) <0.01 <0.01 Cu (Copper) (ppm) 29.63 42.47 Cr (Chromium) (ppm) 6.95 10.95 Cd (Cadmium) (ppm) 1.042 0.89 Mo (Molybdenum) (ppm) 4,866 7.42 Hg (Mercury) (ppb) 1.2 1.0 Ni (Nickel) (ppm) 2.829 6,818 V (Vanadium) (ppm) 11,121 4,113 Co (Cobalt) (ppm) 0.547 0.348 Zn (Zinc) (ppm) 70,056 121,442 Sb (Antimony) (ppm) <0.01 <0.01 ASH COMPOUNDS SiO.sub.2 (%) NS 1.23 Other compounds (%) 22.42 TOTAL (%) NS 23.65

[0228] After passing the slurry through this process, the final pellet of the same was also sampled, delivering the following analytical results, according to Table III:

TABLE-US-00003 TABLE III Unit of Parameter measured measurement Pellets Higher Calorific Power (kcal/kg) 4,550 Lower Calorific Power (kcal/kg) 4,219 Lignin (%) 35.6 Cellulose and hemicellulose (%) 62.7 Particle size (mm) 0.595-0.297 (72% of particles) Total Humidity (%) 6.96 Ash (%) 1.7 RAW MATERIAL COMPOUNDS Sulphur (%) 0.14 Carbon (%) 50.23 Hydrogen (%) 5.97 Nitrogen (%) 0.44 Oxygen (%) NS Mn (Manganese) (ppm) 51 As (Arsenic) (ppm) <0.01 Pb (Lead) (ppm) 12.2 Cu (Copper) (ppm) 13.23 Cr (Chromium) (ppm) 3.13 Cd (Cadmium) (ppm) <0.01 Mo (Molybdenum) (ppm) 7.42 Hg (Mercury) (ppb) 1.2 Ni (Nickel) (ppm) 2.98 V (Vanadium) (ppm) 2.03 Co (Cobalt) (ppm) <0.01 Zn (Zinc) (ppm) 29.49 Sb (Antimony) (ppm) <0.01 Cl (Chlorine) (ppm) 70 ASH COMPOUNDS SiO.sub.2 (%) 1.21 Other Compounds (%) 19.29 TOTAL (%) 20.5

[0229] For the comparative calculation of the reduction of Silicon, it should be taken into account that the percentage of Silicon varies fundamentally in relation to the percentage of Ash, and the latter with respect to the total product.

[0230] The following processes were used for the analyses under international standard conditions as shown in Table IV:

TABLE-US-00004 TABLE IV Test Methods Sample preparation UNE-CEN/TS 14780 EX Applicable: solid biofuels Ash UNE-EN 14775 Elemental analysis (C, EN 15104 H, N) Applicable: solid biofuels Sulphur content EN 15289 Applicable: solid biofuels Determination of major UNE EN 15290 elements in biomass by ICP-OES (Ca, Al, Mg, K, Na, Si, P, Ti, S, Fe) Determination of UNE EN 15297 minority elements in biomass by ICP-OES (Cr, Cu, Zn, Pb, As, Mo, V, Mn, Ni, Cd, Co, Sb) Sample digestion (for UNE EN 15290 majority and minority elements) Determination of UNE-EN 15297, December 2011 Applicable: minority elements in Solid biofuels I-L-094, based on the biomass by Hydride Manual of the AAS AAnalyst 400 Generation AAG Arsenic (quantification) equipment Determination Determination of minor UNE-EN 15297, December 2011 Applicable: elements in biomass by Solid biofuels (digestion) I-L-089, Cold Vapor AAS Determination of Mercury by Cold Vapor Determination of Atomic Absorption Spectroscopy Mercury

[0231] The following Table VIII shows the analyses performed on the reactants and products of the patent application by the same inventor PCT/CL2017/00009.

TABLE-US-00005 TABLE VIII STANDARDS USED ASTM Standard Practice for http://www.astm.org/Standards/D3172.htm D3172-13 Proximate Analysis of Coal and Coke ASTM D4239 - Standard Test Method http://www.astm.org/Standards/D4239.htm 14e2 for Sulfur in the Analysis Sample of Coal and Coke Using High-Temperature Tube Furnace Combustion ASTM D4239 - Standard Test Method http://www.astm.org/Standards/D4239.htm 14e2 for Sulfur in the Analysis Sample of Coal and Coke Using High-Temperature Tube Furnace Combustion UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 14774-1: 2010 Determination of orma.asp?tipo=N&codigo=N0045726#.VxD5C6jh moisture content. DIU Oven drying method. Part 1: Total humidity. Reference method. UNE-EN Solid biofuels. Method http://www.aenor.es/aenor/normas/normas/fichan 14775: 2010 for the determination orma.asp?tipo=N&codigo=N0045971#.VxEDa6jh of ash content. DIU UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 14918: 2011 Determination of orma.asp?tipo=N&codigo=N0046857#.VxD8Bqjh calorific value. DIU UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 15104: 2011 Determination of total orma.asp?tipo=N&codigo=N0048348#.VxD8X6jh carbon, hydrogen and DIU nitrogen content. Instrumental methods. UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 15104: 2011 Conversion of orma.asp?tipo=N&codigo=N0048440#.VxD- analytical results from GqjhDIU one base to another. UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 15148: 2010 Determination of orma.asp?tipo=N&codigo=N0045972#.VxD5hajh volatile matter content DIU UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 15289: 2011 Determination of total orma.asp?tipo=N&codigo=N0048352#.VxEGcqjh sulphur content. DIU UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 15296: 2011 Determination of orma.asp?tipo=N&codigo=N0048507#.VxD2xqjh minority elements. As, DIU Cd, Co, Cr, Cu, Hg, Mn, Mo, Ni, Pb, Sb, V and Zn UNE-EN Solid biofuels. http://www.aenor.es/aenor/normas/normas/fichan 15297: 2011 Determination of the orma.asp?tipo=N&codigo=N0048352#.VxD4tKjh total content of minor DIU elements, mercury, and arsenic

[0232] Particle size was measured under standard EN 15149-1, by the transfer of particles through different sieves and the weight of the material retained in each one for the product that was being measured, in order to calculate the majority percentage retention for a range of particle sizes.

[0233] The measurement of lignin, cellulose and hemicellulose was carried out based on standard ASTM D-1106.

[0234] As can be seen by comparing the results of Tables II and Ill, the step of the washing system achieves toxicity parameters (referring to the chemical elements that can produce risks) that are much lower than those already known, also, in the final pellet silica, particle size and nitrogen levels are achieved that are extremely lower than those of origin.

[0235] Regarding the process, apart from having more efficient steps with respect to washing the fibre and the end product, energy consumption is unusually lower compared to the state of the art with respect to particle size. This is due to the use of energetically passive steps for the fibre washing process. This can be verified comparatively in the following Table V:

TABLE-US-00006 TABLE V Power of installed process equipment kW Installed power Operating kW PCT/ PCT/ ITEMISED CL2017/ Development CL2017/ Development SECTION 00009 Process 00009 Process Purine pump (B) 4 4 3 3 Traditional 4 0 3 0 Extruder Screw (F) Gutter 0 0 0 0 Agitator Tank 4 0 3 0 Screen 102 0 0.25 0 0.1875 Traditional 2 2 1.5 1.5 Extruder Screw 104 Dispenser 106 0.5 0.5 0.375 0.375 Humidifier 110 0.75 2 0.5625 1.5 Cavitating 0 4 0 3 Impingement 120 Ultrasound 8 0 6 0 Ultrasound tank 2.5 0 1.875 0 Screen or Sieve 0 0.25 0 0.1875 158 Rotary Separator 1 1 0 0.75 0 IBC 1 2.2 0 1.65 0 Rotary Separator 2 1 0 0.75 0 IBC 2 2.2 0 1.65 0 Flocculation tank 2.2 0 1.65 0 Water Tank 2.2 2.2 1.65 1.65 Ozone 126 2 2 2.25 2.25 Hammer mill screw 0 7.5 0 5,625 166 Traditional Screw 4 0 3 0 Total 44 26 33 19 Percentage 75% 30% 75% 30% moisture in Biomass Output Percentage 59% 59% decrease in Power kW

[0236] As can be seen, the decrease in energy by the new development is verified as 59%, with a 40% decrease in the percentage of water in the end product obtained.

[0237] When analysing the result above, we consider that the cavitation and subsequent impingement steps are passive steps of lower energy consumption with respect to the ultrasound indicated in the state of the art. On the other hand, the hammer mill screw dehydration step is highly efficient in dehydrating the fibres, leading to a lower energy consumption in the dryer. The product can be compared before the dryer operation of application PCT/CL2017/00009, where the humidity range was between 65% to 75% w/w; on the other hand, the current humidity range handled before the dryer is in the range of 30% to 35% w/w. If you add to this a smaller average particle size range for the current product, it results in almost 71% less energy consumption by the dryer.

[0238] On the other hand, to verify the energy efficiency of the hammer mill screw (j) of this process, the efficiency of the device with respect to its energy consumption was verified, as seen in Table VI:

TABLE-US-00007 TABLE VI Screw hammer mill performance per 100 kg expressed in dry matter heat energy to heat energy to % Moisture kW necessary to evaporate water evaporate water in slurry Kilos of Litres obtain 100 kg dry from 10° C. in from 10° C. in sample Dry Matter of water matter (motor power) Kcal kW 90% 100 900 0.05 570,780 664 85% 100 567 0.08 360,990 420 80% 100 400 0.54 255,780 297 75% 100 300 1.00 192,780 224 70% 100 233 1.46 150,570 175 65% 100 186 1.91 120,960 141 60% 100 150 2.37 98,280 114 55% 100 122 2.83 80,640 94 50% 100 100 3.29 66,780 78 45% 100 82 3.74 55,440 64 40% 100 67 4.20 45,990 53 35% 100 54 4.66 37,800 44 30% 100 43 5.12 30,870 36 25% 100 33 5.58 24,570 29 20% 100 25 6.00 19,530 23 15% 100 18 15,120 18 10% 100 11 10,710 12  5% 100 5 6,930 8  0% 100 — 0

[0239] Table VI shows the great convenience of using the hammer mill screw, because the state of the art discloses, in general, screws that obtain 75% humidity in the end product at a power of 1 kW for every 100 kg of dry matter, which means that 300 litres of water have to be evaporated with an caloric energy cost of 224 kW to obtain the dry matter. The high efficiency hammer mill screw (j) achieves a range of between 30% and 35% moisture in the material with 5.12 kW of power per 100 kg of product at equivalent dry matter and with a quantity of 43 litres of water to evaporate which is equivalent to 36 kW of heat energy. This means that the high efficiency hammer mill screw (j) in this case obtains a caloric energy saving of 184.12 kW.

[0240] Finally, a comparative chemical analysis of the pellets produced by the process closest to the state of the art (PCT/CL2017/00009) and the pellets produced by the present development was carried out, as can be seen in the following Table VII:

TABLE-US-00008 TABLE VII Solid-liquid Product Product separation obtained obtained according to through through the Publication application process of the Parameter Unit of Dung or Raw Number WO PCT/CL2017/ present measured measurement Material 2015086869 A1 00009 development Higher Calorific (kcal/kg) 3,906 3,602 4,545 4,550 Power Lower Calorific (kcal/kg) 3,639 3,350 4,228 4,219 Power Lignin (%) 24.7 NS 28 35.6 Cellulose and (%) 45 NS 67.97 62.7 hemicellulose Particle size (mm) 10-0.595 (67% NS 2-0.595 (84% 0.595-0.297 (72% of particles) of particles) of particles) Total Humidity (%) 8.58 6.18 6.52 6.96 Ash (%) 24.13 24.55 4.03 1.7 RAW MATERIAL COMPOUNDS Sulphur (%) 0.29 0.21 0.11 0.14 Carbon (%) 37.76 36.45 46.62 50.23 Hydrogen (%) 5.14 4.84 6.07 5.97 Nitrogen (%) 2.35 0.91 0.61 0.44 Oxygen (%) 29.99 32.98 41.17 NS Mn (Manganese) (ppm) 295 245 78.81 51 As (Arsenic) (ppm) <50 <50 <50 <0.01 Pb (Lead) (ppm) <50 <50 <50 12.2 Cu (Copper) (ppm) 109 <50 <50 13.23 Cr (Chromium) (ppm) <50 <50 <50 3.13 Cd (Cadmium) (ppm) <50 <50 <50 <0.01 Mo (Molybdenum) (ppm) <50 <50 <50 7.42 Hg (Mercury) (ppb) 1.0 NS NS 1.2 Ni (Nickel) (ppm) <50 <50 <50 2.98 V (Vanadium) (ppm) 55 75 <50 2.03 Co (Cobalt) (ppm) <50 <50 <50 <0.01 Zn (Zinc) (ppm) 131 53 <50 29.49 Sb (Antimony) (ppm) <50 <50 <50 <0.01 Cl (Chlorine) (ppm) 3445.88 740.63 100 70 ASH COMPOUNDS SiO.sub.2 (%) 2.93 7.02 2.89 1.21 Other Compounds (%) 53.18 53.98 45.75 19.29 TOTAL (%) 56.11 61 48.64 20.5

[0241] Based on the results shown above, we show below in Table I the ranges for higher calorific value, lower calorific value, total humidity and relevant toxic compounds expected from the product generated by the method of the present development:

TABLE-US-00009 TABLE I Unit Range Higher Calorific Power (kcal/kg) 4200-5700 Lower Calorific Power (kcal/kg) 4000-5300 Total Humidity (w/w %)  1-10 Ash (w/w %) 0-3 Sulphur (w/w %) .sup. 0-0.2 Nitrogen (w/w %) .sup. 0-0.5 Particle Size (mm) 0.595-0.297
Where (w/w %) corresponds to percentage in dry weight.