WO2022067450A1 - Sistema de lavado de residuos biológicos para su recuperación como biocombustible sólido - Google Patents
Sistema de lavado de residuos biológicos para su recuperación como biocombustible sólido Download PDFInfo
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- WO2022067450A1 WO2022067450A1 PCT/CL2020/050112 CL2020050112W WO2022067450A1 WO 2022067450 A1 WO2022067450 A1 WO 2022067450A1 CL 2020050112 W CL2020050112 W CL 2020050112W WO 2022067450 A1 WO2022067450 A1 WO 2022067450A1
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Definitions
- the present method allows obtaining a product with a high calorific value, low emission of toxic gases and ashes, and low vitrification in the oven or stove when calcined, which corresponds particularly to lignin, cellulose, hemicellulose and their derivatives, with a great energy savings in the process and with low labor intensity in the operation.
- the manure generated can cause negative environmental impacts if there is no control in storage, transportation or application, due to the emission of polluting gases into the atmosphere, and the accumulation of micro and macro-nutrients in the soil and in the superficial water bodies, as a final destination.
- the present development presents a system, a method and a biomass product or derivative with a high calorific value and extremely efficient in contributing to the reduction of greenhouse gas emissions. In practice, it allows the replacement of fossil fuels with biomass. Where in your process production generates significant energy savings and efficiencies in labor intensity.
- the field of application of this system, method and product includes the treatment of waste (solid and semi-solid) of biological origin, in particular the livestock industry, biomass recovery systems for energy generation and biomass drying and preparation processes.
- the livestock sector is responsible for 18% of greenhouse gas emissions measured in CO2 equivalent. This is a higher participation than transportation.
- the livestock sector is responsible for 9% of anthropogenic CO2 emissions. Most of this is derived from changes in land use, especially deforestation caused by the expansion of grasslands for fodder. Likewise, stabled animals, especially cattle, are responsible for the emission of gases with much greater potential to warm the atmosphere. This sector emits 37% of the anthropogenic methane (with 84 times the global warming potential (GWP) of CO2) produced mostly by enteric fermentation in ruminants. It emits 65% anthropogenic nitrous oxide (with 296 times the global warming potential of CO2), mostly through manure. Livestock are also responsible for nearly two-thirds (64%) of anthropogenic ammonia emissions, which contribute significantly to acid rain and ecosystem acidification.
- GWP global warming potential
- livestock sector is responsible for 20% of the terrestrial animal biomass.
- the livestock sector is a key factor in the increase in water use, since it is responsible for 8% of the world's consumption of this resource, mainly for the irrigation of forage crops (FAO Livestock'slongshadowenviromentalissues and options 2009). It is also probably the largest source of water pollution and contributes to eutrophication, "dead" zones in coastal areas, the degradation of coral reefs, the appearance of health problems in humans, the antibiotic resistance and many other problems.
- the main sources of contamination come from animal waste, antibiotics and hormones, chemicals used in tanneries, fertilizers and pesticides used on forage crops, and sediment from eroded grasslands. For this reason, ways to reuse and decontaminate these liquid wastes must be sought.
- both manure and slurry generally correspond to a mixture of animal feces with urine and eventually bedding material, the latter being understood as the place of rest and feeding of the animals.
- Manure in addition to containing feces and urine, can be composed of other elements, such as those present in the beds, generally straw, and also sawdust (or sawdust), wood chips, chemical products, sand, shells, capotillo, remains of the cattle feed, and water.
- sawdust or sawdust
- wood chips wood chips
- chemical products sand, shells, capotillo
- Manure is normally applied on the ground: adding organic matter to the soil.
- the contribution of organic matter supposes an improvement of the structure of the soil, as well as increases the capacity of water retention.
- manure is a rich source of nutritional elements for plants (N, P, K).
- the amount of nutrients and minerals present in the manure depends on various factors, among which the following stand out: Type of cattle, cattle feed (which is directly related to the fate of the animal) and environmental conditions.
- Ligninocellulose is a complex material that constitutes the main structure of plant cell walls and is mainly composed, in the case of cereals, of cellulose (40-50%), hemicellulose (25-30%) and lignin (15-20%). , in the case of grasses (forage consumed by ruminant animals), the average percentages are divided into cellulose (24-39%), hemicellulose (11-39%) and lignin (4-11%).
- Cellulose is a homogeneous linear polymer of 7,000 to 15,000 glucose units linked by glycosidic bonds that are stabilized with hydrogen bonds.
- Hemicellulose is a branched heteropolymer or a linear heteropolymer of between 200-400 units of different pentoses, hexoses and uranic acids with an amorphous structure.
- Lignin is a crosslinked amorphous polymer of three units of p-cumahl phenylpropane, coninect and alcohol.
- ligninocellulose biomass such as wood or agricultural residues (Brethauer, S., & Studer, MH (2015). Biochemical Conversion Processes of Lignocellulosic Biomass to Fuels and Chemicals-A Review.
- silica Another element within the composition of the slurry is made up of significant amounts of silica or its derivatives directly related to the amount of ash existing in its combustion.
- silica also other biological residues with large amounts of silica in their structure, such as rice husks, which, when left as part of the slurry (cannot be digested) or simply as waste, increase the percentage of silica in the final residue.
- silica when the finished products (briquettes, pellets or others) are burned under any process modality, the silica can reach temperatures above its melting point between 1,100 and 1,700°C, vitrifying the surfaces of boilers and ovens, causing them to lose efficiency in heat exchange.
- nitrogen in the form of uric acid, such as ammoniacal nitrogen and other nitrogen derivatives.
- uric acid such as ammoniacal nitrogen and other nitrogen derivatives.
- the distribution in bovine manure is 50% uric acid and 50% ammoniacal nitrogen.
- this concentration is important, however, for the final product of this development in the form of ligno-cellulose briquettes or pellets to be burned, it is a problem.
- the problem is that the generation of N-Oxides (NOx) after a combustion process is already known.
- N-Oxides naturally tend to super-oxidize forming NO3 to form HNO3 with atmospheric water, a corrosive compound that is harmful to health and combustion equipment.
- N2O can be formed, a highly damaging product of the ozone layer and very chemically stable with a half-life of over 170 years.
- the Nitrogen derivatives and percentages that remain in the final product are extremely important at the time of burning because they carry toxic, corrosive and persistent by-products into the environment.
- the patent of the same inventor PCT/CL2017/00009 mentions in its example of table 18, 0.61% w/w of nitrogen in the final product.
- the present development manages to reduce this amount of nitrogen, approximately, by 30% w/w in the final product, based on the operation of the present process presented below. This is due to the fact that chemical reactions take place in the cavitatoha stage, where the O2 from the environment and, to a greater extent, the injected O3 react with the nitrogens of the treated slurry, generating NO. This decreases the final concentration of nitrogen in the final product.
- cattle slurry which are available at a very low cost, but with a non-negligible handling and disposal cost, where also, in order to reduce prices, the use of the product of the treatment of these slurries without prior treatment as fuel or as raw material for fuel.
- a separation method has been described by means of a coagulation-flocculation process, whose separation protocol consists of taking the raw manure stored at 4°C and sifting it to through a 1 mm mesh, then it is subjected to a coagulation/flocculation process according to the following conditions and stages: (1) for the coagulation process, a coagulating solution was added and mixed for 2 min at 175 rpm; (2) for flocculation a solution of polyachlamide is added and mixed for 13 minutes at 50 rpm; (3) formation is expected or settling of the solid, for 2 hours when the supernatant was removed, or for 5 minutes when a filter press is used to separate the solid fraction (Characterisation of solid and liquid fractions of dairy manure with regard to their component distribution and methane production JL Rico , H. Garcia, C. Rico, I. Tejero Bioresource Technology 98(2007) 971-979).
- methane a gas used as fuel.
- the yield and quality of this compound obtained from manure has been studied, expressing its results according to the volatile solids (VS) parameter (Methane productivity of manure, strawand solid fractions of manure H.B. Moller, S.G. Sommer, B.K. Ahring, Biomass and Bioenergy 26 (2004) 485-495).
- VS volatile solids
- Documents WO 2015086869 A1 and ES 2171 1 1 1 A1 present different procedures for the treatment of manure.
- Document WO 2015086869 A1 discloses a process comprising: (a) physical solid/liquid separation in a liquid effluent containing purines (b) physical-chemical separation of the liquid fraction obtained in step (a), to obtain a solid and a liquid fraction (c) electrocoagulation of the liquid fraction obtained in the stage to obtain a solid and a liquid fraction; and (d) pelletizing the solid fractions obtained in step (a), (b) and (c) in the presence of chemical or lignocellulosic materials.
- the solid agglomerate obtained from the pelletizing process offers a high calorific value in combustion, and the resulting liquid has a very low content of nitrogenous compounds.
- the solid fraction has high levels of nitrogen because this element is found in low quantities in the liquid fraction. This results in a high amount of NOx emission, at the moment of burning the pellets, briquettes or any solid form with this residue.
- the NOx when emitted have an unpleasant odor that is part of the odor generated by the pollutants when they are incinerated, such as heavy metals and high concentrations of ashes.
- document ES 2171 1 1 1 A1 presents a procedure and a plant for the treatment of slurry, which includes: (ii) carrying out a physical-chemical treatment on the liquid phase of the slurry to reduce the emission of ammonia content in said purines during the evaporation stage, by means of stripping or fixation by acidification; (ii) subjecting the liquid stream resulting from stage (i) to vacuum evaporation until obtaining a solid concentrate containing between a 20% and 30% by weight of solids; and (iii) drying the concentrate of solids from stage (ii) until obtaining a product with a maximum moisture content of 12%, useful as organic fertilizer, or enriched with a fertilizer ammonia salt.
- WO 201 1/133190 describes a biomass composition, where this composition includes: (i) a lignocellulosic material; and (ii) at least one member selected from the group consisting of potassium, sodium, and chlorides, wherein said at least one member comprises no more than about 0.01% (by weight) of said composition.
- the composition may not include more than 10% water.
- document US 2014/250776 presents a process for converting waste fibers into solid fuel, which includes supplying animal waste, including waste fibers, in a predetermined amount; the flushing of the animal waste supply during a predetermined flushing period; dewatering the animal waste supply by separating the water from the waste fibers over a predetermined dewatering period; stripping waste fibers to separate liquids from solids; compressing the dried and dumped waste fibers to generate a plurality of briquettes; roasting at least one of the plurality of briquettes in a roasting reactor using a heat source at a predetermined roasting temperature for a predetermined roasting period; removing at least one of the plurality of briquettes from the reactor; and cooling the torrefaction reactor to reach a predetermined cooling temperature.
- the material is fed to the system (step a)) by a screw conveyor, the interior of which is in communication with a chamber comprising an ultrasound generator that generates ultrasonic vibrations in the presence of water (steps (b) and c)), causing the material loses its microstructure, and in this state the material is sequentially subjected, while being shaken, to primary crushing, dilaceration and liquid-solid separation (step (d)), compression and separation of components (step (e)) and finally the production of the dry lignocellulosic material (steps f) and g)).
- this patent includes in its process, the expansive explosion of steam, microwaves, heating, a number of extra chemical and biological processes, such as decomposition of cellulose. Finally, the product of This process is mixed with coal dust, to obtain a product with a high calorific value.
- biomass processing method for obtaining ethanol from vegetable stubble is taught.
- biomass eg plant biomass, biomass from animal excreta and biomass from urban waste
- the systems may feed materials such as cellulosics or lignocellulosics, and/or starch or sugar-containing materials to produce ethanol and/or butanol by fermentation, for example.
- sonication breaks the lignin and cellulose bonds, creating bursting bubbles in the medium containing the lignin and cellulose, in order to better expose the bursting debris to biological processes.
- the implosive force increases the local temperature within the bubble to about 5100°K and generates high pressures. It is also indicated that these materials are sonicated with a frequency range of 16 kHz to 1 10 Khz). These high temperatures and pressures break the bonds in the material. Also shown is a general system in which a stream of cellulosic material is mixed with a stream of water in a tank to form a process stream, where a first pump draws the process stream from the tank and directs it to a flow cell. . The ultrasonic transducer transmits ultrasonic energy, causing the physical-chemical process described. It is also stated that, upon separation, the solid material dries out and can be used as an intermediate fuel product.
- Document DE 10200141 16250 also proposes a method for treating a mixture of at least one liquid phase and at least one solid phase, in particular liquid manure or sewage sludge, comprising the steps of: a) generation of an ultrasound field (5.1 b-5). nb); b) the transport of the mixture through the region of the ultrasonic field; c) treating the mixture with ultrasound in the region; and d) separating the mixture into the liquid phase and the solid phase after ultrasonic treatment. It is further proposed that a suitable apparatus be available to carry out the process and use the solid phase generated by the process or apparatus. The objective of this method in general is to reduce the water content for the solid part between 1.8 to 3%, increasing the amount of nitrogen in the solid so that it is a good fertilizer.
- document WO 2013007847 presents a water treatment system with biological waste by means of electrocoagulation and electrooxidation, which consists of the inclusion of slurry in a slurry pool by means of pumping system, where it is exposed to a solid/liquid separator or filter press.
- the process consists of sending the solids to a storage container to be dried by exposure to open air or artificially to obtain fertilizing fertilizers for land, while the liquids are sent to a flotation-flocculation tank.
- sludge is generated and sent to the filter-press, from which it is mixed with the solids from the storage tank, while the liquid material is passed through an electrocoagulation unit for the separation of floating sludge, precipitated sludge and clarified water that is sent to a tank.
- the floating sludge is transferred by decantation to the press filter, while the precipitated sludge is purged, and the treated water goes through a process where caustic soda is added to increase the pH and thus be included in an electro-oxidation stage.
- WO 2009108761 and US 6149694 present processes for producing fuel from organic waste.
- WO20091 08761 A1 discloses a process for producing liquid hydrocarbon fuel from organic medical waste materials based on distillation treatments, through distillation towers or cracking towers. The procedure consists of preparing a suspension from the waste materials to form a torrent, the volume of the torrent is accumulated in a container with agitation. Subsequently, the stream is heated to a temperature between approximately 60-700°C and a pressure between 20-600 psi to decompose solid organic materials and inorganic materials separately.
- document US 6149694 presents a process for forming fuel from livestock waste, which comprises: (i) forming a mixture that has a number of solid components derived from livestock waste and a second waste product different from said livestock residue, where the solid components have a moisture content before said forming step, and where the mixture formed has a moisture content lower than the solid content, and (b) forming the mixture resulting from the stage (a) in a self-sustaining body having a density close to about 20-40 lbs/ft 3 .
- this patent presents a traditional solid/liquid separator by screw or field screen in which about 40 to 60% of sawdust is added to make a pellet, where this product maintains all the contaminants of its source residue, such as, high concentration of ashes, heavy metals, high concentrations of nitrogen, among others.
- Documents CA 2670530, DE 102010019321 and US 20150004654 present procedures for the mechanical separation of liquid and solid components from manure used as raw material to produce fuel pellets.
- document CA 2670530 discloses that said pellet contains approximately 25-75% by weight of cellulosic material (cellulose, lignin and hemicellulose); and approximately between 14-75% by weight of waxed cellulosic material, which corresponds to lignocellulose to which a layer of wax was added.
- the process presented mixes 42% manure with 40% sawdust, cotton, jute, etc. And the remaining percentage with paper, cardboard, or another derivative of paper.
- document US 20150004654 discloses a process for producing biomass and sugar pellets from cellulosic material.
- a process of extracting sugars from wood is described, through hot water and/or steam, and then fermentation. It is a process to raise the calorific value of wood, eliminating the cellulose, to leave it similar to the calorific value of coal. and thus be able to replace a coal-fired boiler, if wood is used, it loses 60% of its heat capacity.
- the objective of the use of the dry products or by-products of the aforementioned processes in general, only points to the production of solids for burning or energy generation.
- the ligno-cellulosic material, as a by-product can also be used as a reactant in processes that do not lead to the destruction of the by-product for energy generation, thus being a form of waste recovery with a higher value. aggregate.
- This development also corresponds to a calorific energy product free of contaminants, free or with minimal amounts of silica monitored through the ash, minimal concentrations of nitrogen and odourless. Being this a fuel product of high calorific value, but coming from animal waste with high levels of silica and high levels of nitrogen, such as manure, among others.
- Cavitation or vacuum aspirations for the present development, the cavitation process is understood as a hydrodynamic effect that occurs when steam cavities are created inside water or any other fluid in a liquid state in which forces respond to pressure differences. , as can happen when the fluid passes at high speed along a sharp edge, producing a decompression of the fluid due to the conservation of Bernoulli's constant. It may happen that the vapor pressure of the liquid is reached in such a way that the molecules that they make up immediately change to a vapor state, forming bubbles or, more correctly, cavities. The bubbles formed travel to areas of higher pressure and implode (the vapor suddenly returns to the liquid state, abruptly "crushing" the bubbles) producing a trail of high-energy gas on a solid surface that implodes, cracking it on impact.
- the implosion causes pressure waves to travel in the liquid at speeds close to the speed of sound regardless of the fluid in which they are created. These may dissipate in the liquid stream or may strike a surface. If the area where the pressure waves collide is the same, the material tends to weaken structurally and erosion begins which, in addition to damaging the surface, causes it to become an area of greater pressure loss and therefore greater focus of vapor bubble formation. If the vapor bubbles are near or in contact with a solid wall when they implode, the forces exerted by the liquid in crushing the cavity left by the vapor give rise to very high localized pressures, causing pitting of the solid surface. Note that depending on the composition of the material used, oxidation could occur with the consequent deterioration of the material. (https://es.wikipedia.org/wiki/Cavitacion)
- Biomass for the present development they will be understood as the waste products of the animal metabolic process, especially that of cattle and pigs, and other elements used for their diet, it can also be understood as the waste product of a bioreactor, which includes a high content of ashes (heavy metals, silica, among others), a high nitrogen content, a high sulfur content, among other parameters that will be seen in the application example.
- Slurry the terms “manure” such as "slurry” such as "dung” to refer to cattle teak.
- the way of collecting and storing the manure does not affect or change in any way the method described or the quality of the solid lignocellulose biofuel obtained from it.
- Regulation refers to compliance with the limit parameters of the ISO 17225-6 standard, and also to the specific parameters of each of the analyzes carried out for this development.
- Silica Refers to silicon oxide, sand and its derivatives, generally between 7 to 12% of bovine feces on a dry basis.
- Nitrogen defined, for this development, as all the nitrogenous material that exists in the aforementioned animal waste, formed broadly by ureic nitrogen, such as uric acid and ammoniacal nitrogen.
- the present development corresponds to a method, system and a product and a by-product for synthesis (or intermediate product) that is obtained or can be obtained, through the treatment of purines that allows obtaining the greatest amount of ligno-cellulose as raw material.
- raw and/or for fuel the largest amount of material cellulose as a product for burning and a by-product for synthesis, for both, with a minimum amount of contaminants, a minimum amount of silica related to the residual ash and a minimum amount of nitrogen.
- the procedure uses organic waste from cattle, which consists of teak and urine and/or manure.
- the present development also corresponds to a method for the treatment of manure that leads to obtaining a high-quality fuel product that efficiently replaces the use of firewood and coal, in boilers for residential or industrial use.
- the purinera is defined as that pool where the feces and urine of cattle arrive.
- the purinera can be composed of other elements, such as those present in livestock bedding (straw and sawdust), waste from biodigesters or bioreactors, digestates, pieces of rubber from rubber blankets, rubber, wood chips, vegetable husks, such as that of rice, chemical products, sand, remains of livestock feed, and water, among many others.
- the material that comes from the (purinera or puhnero well (A) that has a capacity range of between 200 m 3 to 10,000 m 3 , preferably 700 m 3 ) is connected through the passage (1) to the common conveyor screw, with a movement capacity of wet solid material (approximately 95% humidity) of between 150 and 600,000 Kg/h, preferably between 250 and 30,000 Kg/h, with a slight filtering of liquid, where the solid remains with between 70 to 85% humidity (D), which can optionally have a pre-wash through clean water (L), with a flow rate in the range of between 10 and 1000 Its/min in step (30), which is inserted through the upper part of the screw.
- a movement capacity of wet solid material approximately 95% humidity
- step (6) you can, through step (6), enter a grinding (F) with a hammer mill or simple chopper that leaves the solid with a size range of pieces between 5 to 20 mm and go to step (10) where it enters the washing system(l).
- a grinding (F) with a hammer mill or simple chopper that leaves the solid with a size range of pieces between 5 to 20 mm and go to step (10) where it enters the washing system(l).
- step (7) the material goes directly to the washing system (l).
- the Punch Pump (a) with a flow rate range of 80 kg/min to 14000 kg/min, preferably 700 kg/min, preferably 100 kg/min
- the material that has been separated by the Liquid and Solid Separator (C) can be directed through two independent flows, step (4) and step (5).
- Step (4) leads directly to the washing system (l), or step (5), taking it to the hammer mill or simple chopper (F), with a grinding capacity of between 25 to 2000 Kg/min of solid material, preferably 80 kg/min, preferably 43 kg/min) removed lumps, and through step (10), reaches the washing system (l).
- the third system feeding alternative (E) uses the Slurry Pile (E), which corresponds to the one formed by waste from the liquid separators and solids from purineras and/or biogas plants and/or manure accumulation, optionally passing through step (8) to the hammer mill or simple chopper (F) and taken through step (10) to the washing system (I), or from step (9) directly to the washing system (! ⁇
- any of the three alternatives used allows the material to be taken to the washing system (I), without ruling out other undefined alternatives for the entry of slurry into the washing system (I). Within these other input alternatives, it could be the digestates directly from a biodigester or a bioreactor.
- the washing system (I) comprises different associated devices and mutually cooperative stages.
- the first device is the slurry pump (a), (it is included in the system because it requires the initial discharge of the slurry) with a capacity discharge between 80 to 14000 kgr/min, preferably 700 kgr/min, preferably 100 kg/min, which pumps or moves the slurry with a humidity in the range between 80% to 95%, preferably between 84% and 90 %, with a percentage of dry matter of between 9 to 12% w/w from any of the forms of slurry feeding, previously mentioned, to an initial device type screen, sieve or rotary filter (b), which can optionally vibrate, with a light beam of 10 American Mesh (2 mm) up to 40 American Mesh (0.4 mm), preferably 20 American Mesh (0.841 mm) of the filter, which filters and separates a more homogeneous solid product than that provided by the sources slurry delivery, previously mentioned
- the sieve-type device alternative corresponds to a mesh circumscribed to a frame that can optionally vibrate to better extract the water, arranged in a negative inclination.
- the rotary filter type device corresponds to a rotating cylindrical mesh, which is responsible for filtering the flow that passes through it.
- Several of these rotary filters can be arranged in series or parallel, and be washed with external clean water jets. Both the shaker and rotary type filters maintain the same beam of light mentioned previously.
- a lung feeder screw device which is a common solids drive screw with a material displacement capacity of between 500 to 2000 Kg/hr, preferably 1000 Kg/hr, with which the solid is moved to feed a dosing device (d) that portions and standardizes the amount of solid, between 500 Kg/h up to 7000 Kg/h , preferably 1000 Kg/h to enter the next device.
- the humidity of the product is between 60% and 35%, preferably 45% w/w.
- the dosing device (d) for example a basket, screw, rocker, which generally corresponds to a system to regulate the dosage of the material with a required pressure, where, for example, it can be a preprogrammed funnel-type bucket to release its content upon reaching a pre-programmed weight. It mainly consists of an electro-mechanical control system for the dosage and release of the material to be measured.
- ozone O3
- the washing and humidification tank (e) also includes, in the center, a tubular paddle agitation device (e3) that, when turning, generates a centripetal effect of rotary movement that sucks the mixture from the bottom of the tank into its interior and releases it through the upper part of the tube, where also on the other hand, the washing water of the first injection (e1) generates a torrent that drags the solid separating it in combination with the effect of the previously mentioned centripetal movement.
- the content of the washing and humidification tank (e) can be simply centrifugally agitated from the center through paddles with the respective washing water from the first inlet (e1), generating a stream that drags and separates the solid.
- washing and humidification tank (e) After this, if there is an excess of liquid in the washing and humidification tank (e), it 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 puhnera or puhnero well (A).
- the washing and humidification tank (e) also fulfills the function of homogenizing and degassing the excess Ozone (O3), after this and continuing with the process, the transfer of solids is channeled directly from the washing and humidification tank.
- cavitator pumps with a flow capacity, per cavitator, of between 100 and 3000 It per minute, preferably 800 It per minute per cavitator, with powers between 2 to 50 Kw, preferably and by way of example without wanting to restrict other capacities of the system, 4 Kw/h to be able to process between 400 and 1500 Kg/hour of slurry with a range between 85% and 99% of moisture on dry basis, preferably 90%, preferably 97%, preferably 98%, preferably 99%, preferably to process 500 Kg/h of fibers.
- the ozone-water mixture is prepared in an attached ozone preparation tank (o), where the ozone is bubbled through ozone generating machines (p) in a volume of water (J) between 1000 It/h up to 320,000 It/h, preferably 100 to 14,000 lt/min, preferably 1,000 lt/min.
- the origin of the continuous flow of water (J), is the same as that mentioned in the patent of the same inventor PCT/CL2017/00009, where the water (J) that enters the Washing and humidification tank (e) after passing through the attached ozone preparation tank (o), is driven by the liquid booster pump (N) that enters through the upper inlet step (13), and lower inlet step (27), which come from the liquid booster pump (N) which is supplied by step (26), coming in turn from the accumulator and purifier tank (J), which is supplied by step (28), and by step (15) which comes from the filtrates of the entire washing system (I).
- the wash water purification and accumulation tank (J) generates a flow that is represented by step (24) and that feeds the biological material concentrate tank and inert impurities (G), which will be treated to leave them as compost.
- the aforementioned biological material and inert impurity concentrate tank(s) (G) are also fed by the liquid waste generated by the final granulometry filtering (h), the gases bubbled from the cavitation and shock tank (g) and the hammer mill screw (j), which corresponds to step 14, as can be seen in figures 2 and 3.
- the cavitator pumps (g1) are proportional to the number of jets that the liquid to be treated passes through the cavitating ducts (g2), this means that, if the jet passes through a cavitating duct (g2), it necessarily has to be driven by a pump or several jets, by a pump of greater power.
- the cavitating ducts (g2) can operate in series or in parallel, depending on the layout of the system, it can be one or “n” depending on the amount of product to be processed, preferably one cavitating duct, or preferably two cavitating ducts.
- the cavitation and shock tank (g) comprises a series of components that will be described below, firstly, it comprises the cavitating duct(s) (g2), as described in figure 4, which in turn comprise two main structures connected to each other, the cavitation and laminar flow duct (g2a) and the shock duct (g2b).
- the cavitation and laminar flow duct (g2a) comprises a tubular structure with internal and external diameter decreases (external decreases may be optional), with an internal diameter between 4 cm and 22 cm, preferably 6 cm, preferably 1 1 cm, with a total length between 50 cm and 280 cm, preferably 75 cm, preferably 137 cm.
- the materials with which this duct is made include different types of metals resistant to abrasion and oxidation, such as steel and alloys, they can also be polymers, such as polyamide, among others, or there can be a combination of materials in the same duct.
- the cavitator duct (g2) comprises three sections, ordered from where the waste flow enters to its exit in the final granulometric filtrate (vi).
- the cavitation duct (g2) is fed from the washing and humidification tank (e) passing through the cavitation pump(s) (g1), where these residues enter through the diameter of the inlet duct (g2ad) in the first nozzle section (g2aa) where the internal diameter of the cavitating duct (g2) is reduced with a nozzle angle of between 15° and 35°, preferably 21°.
- This reduction in the internal diameter (g2ae) of the cavitating duct (g2) ranges from a slight reduction in the internal diameter of the cavitating duct inlet (g2) to 1/5 of the internal diameter, preferably 1/3.
- This section has a length between 7 cm to 41 cm, preferably 107 cm, preferably 1 10 cm.
- this flow head section (g2ab) which maintains a constant internal diameter in relation to the decrease in internal diameter of the previous section, where this flow head section (g2ab) comprises a length between 4 to 23 cm, preferably 6 cm, preferably 11 cm. In this section a high flow rate is maintained at a constant pressure.
- the third and last section of the diffuser (g2ac) where the internal diameter of the cavitating duct (g2) is widened again at an angle between 5° and 10°, preferably 7° , until reaching to the same inlet diameter (g2ad) of the cavitating duct (g2), where the length of this section ranges from 22 cm to 124 cm, preferably 33 cm, preferably 49 cm.
- the cavitation effect occurs because when the fluid comes with a high flow rate (high speed) and passes through the edge of the angle that is formed when the diameter of the duct expands, a sudden drop in pressure is generated, this drop in pressure generates microbubbles in the fluid and their coalescence, managing to agitate the fibers, agglomerates and particles mixed in the fluid, preferably silica particles, preferably waste derived from nitrogen, derived from sulfur, derived from heavy metals such as cadmium, mercury, lead among others, and waste fibers.
- the inlet pressure to the cavitator duct (g2) can go from a constant pressure to 25% of that pressure in milliseconds, preferably 50%. , as an example, and without being restricted to other ranges, from 4 atmospheres to 0 atmospheres of pressure at the output of this section.
- the process carried out in the cavitating duct (g2) does not consume energy and, through a physical process, efficiently separates the fibers, the silica and the rest of the components of the treated waste, in order to deliver a pre-processed product to the final granulometric filter (h), so that it, in turn, achieves maximum cleanliness.
- shock duct g2b
- This shock duct (g2b) comprises three sections, where the first section maintains the same internal diameter as the inlet (g2ae) to the cavitating duct (g2) and is called the separation section (g2ba), where the flow is partially retained maintaining a laminar flow and it is given a physical space so that the component elements of the waste are separated.
- This section comprises a length of 14 cm to 76 cm, preferably 20 cm, preferably 30 cm.
- the second section of the shock duct (g2b), continuing with the flow, corresponds to the outlet reduction section (g2bb), where the inlet diameter (g2ad) is reduced to a larger diameter (g2bd), with respect to the diameter reduction (g2ae) of the flow load section (g2ab), in the range of between 45% and even slightly less than the internal diameter of the cavitating duct (g2), preferably by 50%, the length of this section is between 2 cm and 1 1 cm, preferably 3 cm, preferably 5 cm.
- the angle of the reduction in this section is of the order of between 25° and 35°, preferably 30°. This section, although it reduces the diameter of the duct outlet (g2bd), comes with a reduced pressure, so it does not generate greater resistance and additional pressure variations.
- the outlet section (g2bc) which can be directed, which will guide the outlet stream of the residue to the final granulometric filter (h).
- This section maintains the reduced diameter of the previous section and comprises a length of between 1 cm and 7 cm, preferably 2 cm, preferably 3 cm.
- two outlet jets are made to collide with each other, or an outlet jet against one of the walls of the tank, or against a sheet or deflector from shock ducts (g2b), where the direction of impact 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, preferably 2 cm, preferably 10 cm, preferably 50 cm, preferably 100 cm , preferably 150 cm, where the ability to shred the fibers of the jets is indirectly related to the distances between the shock ducts (g2b), in other words, the smaller the distance, the greater the shredding.
- an optional piece is presented, which confronts the two shock ducts (g2b), called the directing and shock tube (g2h), which consists of a tube with the same outlet diameter as the discharge duct. shock (g2b) but with two lateral perforations (g2f) and a lower central perforation (g2g) that meet the objective of channeling the explosion of the jet as seen in figure 5.
- the outlet flow of the shock ducts (g2b) is of the laminar type and is in the range of 20 liters per minute to 5000 liters per minute, preferably 500 liters per minute.
- the cavitation and shock tank (g) also includes in its upper part a gas outlet duct (g3d) that channels and bubbles the gases in the tank of concentrated biological material and inert impurities ( G), in order to enrich this residue with the dissolved gases generated in the cavitation and shock tank (g) through step 14.
- the cavitation and shock pond device also comprises an outlet for the product (g3a) of the flow shock, a handle (g3b) for maintaining the cavitating ducts and a viewer (g3c) for verifying the operation of the device.
- the product that comes out of the shock has a humidity in the range of between 85% and 99% p/p on a dry basis, preferably 90% p/p, 98% p/p and 99% p/p.
- the product resulting from the clash of flows falls and is positioned on the final granulometric filter device (h) which corresponds to a final device type screen, sieve or rotary filter (h), which can optionally vibrate, with a beam of light of the fi Itrage of between 0.25 to 2 mm (10 to 60 American mesh), which filters and separates a more homogeneous and finer solid product than the one delivered by the previously mentioned cavitation and shock tank device (g), with a humidity range between 70% and 90%, preferably 83%, where the moistened fibers are retained and the liquid is filtered a second time with its respective contaminants.
- This device is arranged at an angle ranging from 10° above the horizontal to 80° above the horizontal, preferably 45°.
- the screen, shaker and rotary filter type devices are similar to those described for the first granulometric filter.
- the solid retained in this final filter can be sprinkled with recycled water (J) or clean water (L) before going to the next device.
- the solid that falls from the shock of the flows is deposited by gravity in the hammer mill screw device (j), where this device is a compact piece of equipment that operates with two elements, firstly, an extruder mill element and secondly, a hammer mill element.
- the first element of the extruder mill is made up of the following elements related to each other, initially the solid falls by gravity and enters through the input hopper (j6), this hopper channels the solid through the screw axis (j1) which displaces the solid against the tightening system (j8).
- the screw axis (j1 ) in turn is made up of a pipe with a continuous helix (j1 a) with a turning angle that goes from 15° to 50°, preferably 20° and with a distance preferably 15 cm between turns, without wanting to restrict other efficient possibilities with this measure, it also comprises two terminal bushings for the pipe (j1 b), with an internal pipe reinforcement (j1 c), all mounted on a shaft (j1 d ), with a shaft end bushing (j1 e).
- the screw shaft (j1) is also supported on the extruder screw element of the hammer mill screw device (j) by a rear support (j2) and mounted on two conical circular bearings (j3) to maintain the movement of the screw shaft (j1). ), these bearings are held to prevent their exit following the line of the axis, by the clamping sleeves (j5), in parallel an o-ring (j4) separates these bearings (j3) from the material entering the input hopper (j6 ).
- this screen device (j7) includes the same circular screen (j7a) with between 80 and 1000 plates, preferably 1 12, with measurements, by way of example without restricting these measurements, 400 mm long, 30 mm wide by 2.5 mm thick, with a light beam between 0.05 and 3 mm, supported on a screen support (j7c) and wrapped in the screen envelope (j7b), which fulfill the function of channeling the water extracted in the tightening and channeling it through the drain (j7f) to its recirculation, retaining the solid in the inner surface of the screening device (j7).
- This sieve device (j7) is easily removable by means of the sieve handle (j7e) for cleaning, where in addition to being able to extract the sieve itself (j7a), the device cover (j7d) can be removed.
- the aforementioned tightening system (j8) comprises an area delimited by the covers: upper (j22), upper side (j23) and lower side (j20) that support the accumulation of chopped solid material by means of the blades (j8e) that They are tightened on the blade holder (j8a), which in turn is stabilized on the axis horizontally by the spring (j8c), which in turn exerts pressure against the direction of the material by the screw axis (j1).
- the clamping system to be attached to the extruder mill element of the hammer mill screw device (j), is mounted through a lever-holder (j8b) that holds the lever (j8d), which supports the clamping system (j8) to the total device in an easy and removable way in case it is necessary to replace the blades (j8e).
- This tightening system (j8) remains in a firm position without turning, but allows the screw axis (j1) to rotate freely, causing the retained solid to be squeezed, increasing the runoff time, leaving a more dehydrated solid material.
- the tightening system (j8) compresses and chops the solid and when it accumulates in part on the screw axis (j1), it releases liquid in the sieve device (j7).
- Most of the solid falls due to pressure and gravity to the grinding assembly (j14) or to a traditional hammer mill that corresponds to the second element of the hammer mill screw device (j), where this grinding assembly (j14) is constituted by a support box (j14c) and a circular outlet for solid material (j14b), internally it comprises a set of grinding or shredding blades in the shape of a symmetrical cross (j14a) mounted on a tube (j14 ⁇ ), which rotates on a square grinding shaft (j14h), where for this rotation, the grinding shaft (j14h) is positioned between two square base bearings (j14d) at each end of the tube outside the box.
- the blades rotate due to the energy delivered by the rotation of the pinion (j14f) and by the pressure exerted by the solid when it wants to come out due to the restriction generated by a grid (j14g) with a beam of light slightly greater than the thickness of the blade.
- a grid j14g
- a beam of light slightly greater than the thickness of the blade.
- the grinding assembly In order for the grinding assembly to be in position and rotate freely on its shaft, it is also contains a grinder assembly support bearing (j14e), which is mounted in the grinder assembly support (j17).
- This motor is directly associated through the standard shaft of the motor (j13) to the shaft (j1 d) to deliver the rotation to the entire device, with a speed between 10 and 250 rpm.
- this motor can have a capacity of 10 Hp and a speed of 140 rpm, without restricting the capacity and power of the motor to this example specifically.
- the motor is supported on the motor base (j18) and positioned by the motor support (j15).
- the efficiency of the hammer mill screw device (j) is such that it begins working with solids with humidity around 85% p/p and after all the milling, pressing, cutting and filtering processes, it arrives at a mixture of fibers with a humidity below 30% p/p, which results in lower energy consumption in later stages to efficiently dry the final product.
- the size of the final fiber is also in the range of 0.595 - 0.297 mm, taking into account 72% of the total sample, which provides a greater surface for exposure to oxidants and fire in the final combustion of the product, thus improving the efficiency of the final combustion.
- step (16) The solid material is transported through step (16) to the pressing or centrifugation section (O), which removes excess water from the material, which, subsequently, is taken through step (18) corresponding to a dryer (P), which is fed with hot air through the passage (21) which in turn is fed by the Boiler (Q), then this material falls through the passage (19) in a vibratory screening device dry magnetic (S) that corresponds to a shaker-type device, similar to the one indicated in stage (b) of the washing system (I) but dry, with magnetic bars to trap metals and a sifting light beam of between 2 mm (10 American mesh) up to 0.595 mm (30 American mesh), which sieves and separates a fine homogeneous powder-type solid product with a humidity range of between 10% and 5%, preferably 7%, where the fragments of larger size and the sifted powder is channeled through pneumatic ducts (20) to the pelletizing process (T).
- This device is arranged at an angle ranging from 10° above the horizontal
- the material that has been processed is incorporated into the Pelletizing process (T) through step (20) to finally form pellets and/or ligno-cellulose briquettes and/or some other solid form to be burned.
- This development in addition to cleaning the fiber of all kinds of impurities on the outside, is also capable of cleaning the fiber on the inside, which is full of bacteria, enzymes, gastric juices that are responsible for dissolving cellulose and hemicellulose to transform them. in sugars, but when they leave the animal they remain inside the fiber as contaminating matter and when burned they emit odors and gases that are harmful to health.
- This development is also capable of cleaning the fiber inside and out of silica residues, thus improving the final product by eliminating its vitrification capacity inside boilers and stoves.
- this system manages to remove all contaminants both inside and outside of the solid components of the slurry and its mixtures, in a continuous process eliminating its contaminants, leaving a solid product with particular characteristics.
- chemical agents is not an option for the present development.
- the modifications made to the washing system (I) and its sub-stages in the total performance of the system are a fundamental part of this development.
- the sub-stages of the washing system process (I) include: i) impulsion through the Puhnera Pump (a): movement of the slurry from the puhnero well (A) moving the slurry mixture;
- this sub-stage corresponds to an initial filtering by means of a screen, shaker or rotary filter to standardize and slightly reduce the humidity of the solid in the process, in general a solid with a humidity lower than 85% is received w/w The solid obtained is transported by lung screw where the humidity percentage decreases below 80% p/p; iii) dosage, this sub-stage corresponds to the measurement of the weight of an amount of solid to enter the next sub-stage of the process.
- the weight of a quantity of solid is measured by means of an automated basket and its content is released into the washing and humidification tank (v); iv) centripetal or centrifugal movement with water turbulence and optional injection of ozone, we mention these three sub-steps because they take place inside the washing and humidification tank (e).
- the fiber-containing mixture is rehydrated through the water inlet (J) which moves and drags the fiber-containing mixture, in parallel as a first alternative, in the center of the tank a tubular paddle agitation device sucks this hydrated mixture and raises it by centripetal motion to the top of the apparatus where it spills into the center of said pond.
- a second alternative is simply an agitator blade in the center of the tank, generating a centrifugal effect in the mixture.
- a premixed ozone water mixture can be added to the pond to remove microbiological material and nitrogen-derived compounds, sulfur-derived compounds and other compounds in subsequent sub-stages.
- the ozone-water mixture is prepared in an attached ozone preparation tank (o), where the ozone is bubbled through ozone generating machines (p) in a volume of water (J) of between 1000 It/h up to 320,000 It/h, preferably 33,000 It/h, until reaching a concentration in the range of 900 to 1,200 ppb and this mixture, in turn, is reinjected into the washing and humidification tank (e), as previously mentioned.
- cavitation and shock in this sub-stage, the liquid that leaves the washing and humidification tank (e), is raised by the cavitation pumps (g1) previously described, and the flow passes through the cavitation and shock tank (g ), where through the cavitation duct (g2), the physical reaction of cavitation takes place within the liquid and within the retained moisture contained in the fibers, doing a very high-speed microbubbling job, managing to mechanically destabilize the contaminants. and the different types of fibers within the mixture, being ready for their separation in the shock, between different flows that come from different cavitation ducts (g2) or a single duct and a wall of the cavitation and shock tank (g).
- This substep separates into three phases, the first phase, flow cavitation; the second phase, separation and lamination of the flow; and the third phase, flow shock; vi) final granulometric filtering: this sub-stage occurs after the shock sub-stage inside or against the cavitation and shock tank (g), where the wet solid passes by gravity through a final granulometric filter (h), which corresponds to a final filter by means of a screen, shaker or rotary filter, which retains the moistened fibers and filters the liquid for a second time with its respective contaminants, in general the moistened fibers comprise a humidity between 80 and 85%; and vii) dewatering by hammer mill screw: the wet solid from the previous sub-stage enters a hammer mill screw (j) with a configuration of two elements that first proceeds to push the solid and squeeze it through the extruder screw element which dehydrates it until it is left with a mixture of fibers with humidity below 30% p/p, and then the second element of the hammer mill
- a cavitation pump power (g1) in a range of 2 Kw to 50 Kw is handled, preferably and by way of example without wanting to restrict other system capacities, It is 4 Kw to be able to process 1200 kg/h of slurry at 80% humidity or higher, leaving the fiber diluted in the range of 0.5% to 5%, preferably 2%, preferably 2.5%, preferably 3%, in water, which is the ideal medium for the cavitation stage, with flow rates, for example, of 500 lt/min passing through the cavitator tube (g2).
- the fluid to be treated has a predetermined humidity and dilution to be able to operate in the cavitator tube (g2), where within these parameters the ideal is a humidity of 97% and a particle size of no more than 20 mm.
- stage (vii) uses the hammer mill screw device (j).
- This screw is also a drying screw because it not only manages to move the fibers to the subsequent drying stages, but also extracts the water from the mixture from 98% to 30% p/p, (The state of the art generally mentions that the screws, in general, leave between 70 to 80% moisture in the mixture), which saves time and energy in drying the fibers in later stages.
- This screw can be used in other drying or humidity reduction processes regardless of the method and field of application of this development.
- the hammer mill screw device (j) operates at a high speed between 20 Rpm to 200 Rpm, preferably 140 Rpm, preferably 70 Rpm, in a small diameter and with fiber breaking inner knives, as mentioned earlier in its description.
- the particle size exiting the hammer mill screw device (j) is in a range below 0.595 - 0.149 mm.
- this comprises, according to Table I:
- Figure 1 presents a block diagram of the state of the art of application PCT/CL2017/00009 for the treatment of slurry to obtain lignocellulose as raw material and/or fuel and other chemical components. Operations are shown in blocks, lines of flow or streams are presented with arrows which indicate flow direction, and are also represented with numbers.
- G tank for biological material concentrate and inert impurities
- g cavitation and shock tanks
- g1 cavitator pumps
- g2 cavitator ducts
- g3d gas outlet duct
- h final device type screen, sieve or rotary filter
- j screw device hammer mill
- p ozone generating machines or: attached ozone preparation tank
- This figure shows the cavitation and shock tank (g), its cavitating duct (g2a), the relationship of its internal components, between the cavitation and laminar flow duct (g2a) and the shock duct (g2b) and its different parts. .
- This figure shows the impact angle of the jets coming out of two shock ducts (g2b) and how they behave when they exit the device.
- FIG. 1 shows the hammer mill screw device (j), where all its parts and pieces are shown, where the numerals indicate: j1: screw shaft j1 a: pipe with helix j1 b: terminal bushings of the pipe j1 c: internal reinforcement j1d: shaft j1 e: shaft end bushing j2: rear support j3: circular bearings j4: o-ring j5: clamping sleeves j6: inlet hopper j7: screen device j7a: circular screen j7b: screen surround j7c: screen support j7d: device cover j7e: screen handle j7f: drain j8: tightening system j8a: knife holder j8b: lever holder j8c: spring j8d: lever j8e: blades j9: bearing j10: large pinion j11: small pinion j12: reduction motor j13: standard motor shaft j14: grinding assembly j14a:
- This example was developed in the purineras of the Las Garzas agricultural laboratory. On August 17, 2020, 5450 Kg of beef slurry were used mainly and the procedure of this development was applied. The cleaning water used comes from a well in the area, with water with a high content of dissolved salts.
- the measurement of the particle size was carried out under the EN 15149-1 standard, through the transfer of particles by different sieves and the weight of the material retained in each one of them for the product that was being measured, in order to Calculate the majority retention percentage for a range of particle sizes.
- the stage of the washing system achieves much lower toxicity parameters (in reference to the chemical elements that can cause risks) than those already known, it is also achieved in the final pellet silica, particle size and nitrogen levels extremely lower than those of its origin.
- Table V new development of 59% and a 40% decrease in the percentage of water in the final product obtained.
- the cavitation and subsequent shock stages are passive stages or those with lower energy consumption compared to the ultrasound indicated in the state of the art.
- the hammer mill screw dehydration stage is highly efficient in dehydrating the fibers, subsequently resulting in lower energy consumption of the dryer.
- the product can be compared before the dryer operation of the application PCT/CL2017/00009, where the humidity range was handled between 65 - 75% p/p, on the other hand, the current humidity range handled before the dryer it is in the range of 30 to 35% w/w. If we add to this a lower average particle size range for the current product, it results in almost 71% less energy consumption of the dryer.
- Table VI shows the great convenience of using the hammer mill screw, because the state of the art generally presents screws that obtain 75% moisture in the final product at a power of 1 kW per 100 Kg of material. dry, this means that it is necessary to evaporate 300 liters of water with an energy cost of 224 kW of heat to obtain the dry matter.
- the high-efficiency hammer mill screw (j) achieves a range between 30% and 35% moisture in the material with 5.12 kW of power per 100 Kg of product to equivalent dry matter and with a quantity of 43 liters of water to evaporate which is equivalent to 36 kW of heat energy.
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- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Treatment Of Sludge (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Description
Claims
Priority Applications (11)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/CL2020/050112 WO2022067450A1 (es) | 2020-10-02 | 2020-10-02 | Sistema de lavado de residuos biológicos para su recuperación como biocombustible sólido |
EP20955481.5A EP4223397A4 (en) | 2020-10-02 | 2020-10-02 | SYSTEM FOR WASHING BIOLOGICAL WASTE FOR RECOVERY AS SOLID BIOFUEL |
AU2020470809A AU2020470809A1 (en) | 2020-10-02 | 2020-10-02 | System for washing biological waste to recover same as solid biofuel |
CA3194066A CA3194066A1 (en) | 2020-10-02 | 2020-10-02 | System for washing biological waste to recover same as solid biofuel |
PE2023001340A PE20231723A1 (es) | 2020-10-02 | 2020-10-02 | Sistema de lavado de residuos biologicos para su recuperacion como biocombustible solido |
CN202080106740.7A CN116529344A (zh) | 2020-10-02 | 2020-10-02 | 用于洗涤生物废物以回收该生物废物作为固体生物燃料的系统 |
MX2023003760A MX2023003760A (es) | 2020-10-02 | 2020-10-02 | Sistema de lavado de residuos biologicos para su recuperacion como biocombustible solido. |
US18/029,921 US20230374403A1 (en) | 2020-10-02 | 2020-10-02 | System for washing biological waste to recover same as solid biofuel |
US18/191,381 US20230303938A1 (en) | 2020-10-02 | 2023-03-28 | System for washing biological waste to recover same as solid biofuel |
ZA2023/04713A ZA202304713B (en) | 2020-10-02 | 2023-04-24 | System for washing biological waste to recover same as solid biofuel |
CONC2023/0005500A CO2023005500A2 (es) | 2020-10-02 | 2023-04-28 | Sistema de lavado de residuos biológicos para su recuperación como biocombustible sólido |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PCT/CL2020/050112 WO2022067450A1 (es) | 2020-10-02 | 2020-10-02 | Sistema de lavado de residuos biológicos para su recuperación como biocombustible sólido |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US18/191,381 Continuation US20230303938A1 (en) | 2020-10-02 | 2023-03-28 | System for washing biological waste to recover same as solid biofuel |
Publications (1)
Publication Number | Publication Date |
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WO2022067450A1 true WO2022067450A1 (es) | 2022-04-07 |
Family
ID=80949139
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/CL2020/050112 WO2022067450A1 (es) | 2020-10-02 | 2020-10-02 | Sistema de lavado de residuos biológicos para su recuperación como biocombustible sólido |
Country Status (10)
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US (2) | US20230374403A1 (es) |
EP (1) | EP4223397A4 (es) |
CN (1) | CN116529344A (es) |
AU (1) | AU2020470809A1 (es) |
CA (1) | CA3194066A1 (es) |
CO (1) | CO2023005500A2 (es) |
MX (1) | MX2023003760A (es) |
PE (1) | PE20231723A1 (es) |
WO (1) | WO2022067450A1 (es) |
ZA (1) | ZA202304713B (es) |
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- 2020-10-02 CN CN202080106740.7A patent/CN116529344A/zh active Pending
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AU2020470809A9 (en) | 2024-06-06 |
CN116529344A (zh) | 2023-08-01 |
US20230303938A1 (en) | 2023-09-28 |
AU2020470809A1 (en) | 2023-06-08 |
MX2023003760A (es) | 2023-05-03 |
EP4223397A1 (en) | 2023-08-09 |
EP4223397A4 (en) | 2024-06-26 |
ZA202304713B (en) | 2023-11-29 |
CO2023005500A2 (es) | 2023-05-19 |
US20230374403A1 (en) | 2023-11-23 |
CA3194066A1 (en) | 2022-04-07 |
PE20231723A1 (es) | 2023-10-24 |
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