BR102018003828A2 - SOLID WASTE AND BIOMASS DEHYDRATION AND DENSIFICATION PROCESS AND DEVICE - Google Patents

Abstract

The present technology refers to a process of dehydration and densification of solid waste and / or biomass. The process is an alternative for the treatment of municipal solid waste that is currently mostly stored in a landfill, leading to immeasurable environmental damage. In addition to being a waste treatment process, the claimed method also allows obtaining combustible material. The invention further relates to a device containing a pallet to cover the floor of the dehydration chamber.

Description

PROCESS OF DEHYDRATION AND DENSIFICATION OF SOLID WASTE AND BIOMASS AND DEVICE [01] The present technology refers to a process of dehydration and densification of solid residues and / or biomass. The process is an alternative for the treatment of solid urban waste that is currently, in most cases, stored in a landfill, which can lead to immeasurable environmental damage. In addition to being a waste treatment process, the claimed method also allows obtaining combustible material. The invention also relates to a device containing a platform to cover the floor of the dehydration chamber.

[02] It can be considered that energy consumption and the rate of generation of solid urban waste per inhabitant are directly proportional to the development of a country. Waste becomes a problem and an unsustainable condition when its production goes beyond the treatment capacity and environmental disposal, one of the great challenges of the public authorities is the proper management of solid waste. In Brazil, 79.9 million tons of solid urban waste are generated annually and, of this total, almost 30 million tons are disposed of in dumps or controlled landfills. These locations are considered inappropriate, as they do not have the necessary measures to avoid environmental damage.

[03] When disposed of inappropriately, urban solid waste can cause significant environmental problems, such as leachate and percolate production. In general, these products have high concentrations of organic matter and ammoniacal nitrogen, which are potentially toxic and can trigger a process of contamination of soil and aquifers.

[04] Another form of solid waste management currently used is recycling. Recycling reduces the need for raw materials and

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2/26 energy consumption in industrial production, in addition to reducing social and environmental impacts. It is important to note that the recycling process has some conditions for its real functioning, among them the segregation of waste at the source. The mixture of domestic leftovers, for example, contaminates materials in contact with other residues, making recovery difficult.

[05] Urban solid waste can be used for energy use or for the production of fuels, as they consist largely of paper / cardboard, plastics, textile and organic waste. These materials, present in a large proportion, contain calorific value. Inert materials, such as glass and metal, are also present in waste. The thermal and mechanical treatment to reduce the moisture content and increase the density of these residues can allow a lower generation of pollutants and generate reusable by-products with significant energy content.

[06] The production of briquettes from solid waste has been used as an alternative to increase energy density and decrease volume, facilitating the storage and transportation of these materials. To meet the specifications of the process, the moisture content and granulometry of the residues need to be controlled, therefore, the basis of the method is dehydration by means of heated air flow. Briquettes can be used as fuel for boilers, commercial and industrial ovens, and other sectors that need calorific fuel for production.

[07] The compaction of solid urban waste can also be done from the pelletizing process. The transformation of biomass into pellets is linked to the physical properties of the waste and to variables such as pressure and temperature. Pellets have low moisture content and dimensions that

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3/26 guarantee greater ease of storage, transport and supply of boilers and ovens.

[08] In 2016, the second most important source of generation in the Electricity Supply was biomass, with a record of 8.8% (Portal Brasil, 2017). According to the Monthly Energy Bulletin (reference January / 2018) in 2017, the record increases to 9% showing that sustainable energy production techniques are gaining space on the national scene.

[09] Biomass in the form of biogenic waste, such as sugar cane bagasse and organic materials of vegetable or animal origin in urban solid waste, including paper, cardboard, wood and food waste, are renewable due to their photosynthetic origin. Mineral residues (plastics, rubbers) must be considered as emitters of carbon dioxide when burning. However, when comparing energy use with the option of disposal in landfills or recycling, energy is obtained from the former that would not occur directly in the others, and this additional energy will displace conventional energy sources, allowing a reduction in emissions of carbon dioxide, responsible for global warming.

[010] Documents describing processes for obtaining briquettes and pellets from waste were found in the state of the art.

[011] The Thesis entitled “Properties of briquettes and pellets produced with solid urban waste”, 2014, describes the main characteristics of solid urban waste as well as the properties of briquettes and derived pellets. In the document it is mentioned that one of the difficulties in using waste is its moisture, since excess water can cause problems during the burning process, such as weak ignition and reduced combustion temperature. It is still pointed out in the document that one of the main reasons why

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4/26 municipal solid waste is not widely used is the lack of information on the characteristics of materials and the implications of emissions. The residues used in the study were only tree pruning residues, used corrugated cardboard, used aseptic boxes and water treatment sludge. Even with this waste sorting step, it was necessary to dry the material, which was carried out in an ambient condition with daily turning over for 10 days, a time that makes the use of such a process in an urban waste treatment routine, continuously generated, impracticable. and in large quantities (SOUZA, MM DE. Properties of Briquettes and Pellets Produced With Solid Urban Residues. Doctoral Thesis. Universidade Fedaral de Viçosa, 2014).

[012] The article by Brand MA and collaborators, entitled “Production of briquettes as a tool to optimize the use of waste from rice cultivation and industrial processing ', published on March 27, 2017, describes how to obtain Briquettes from ash rice husk; rice husk and rice straw, that is, an extremely selected sample. These materials were subjected to briquetting without prior treatment, however, for samples with humidity greater than 10%, the briquettes formed lose consistency when leaving the machine (BRAND, MA; JACINTO, RC; ANTUNES, R .; CUNHA, AB DA Production of briquettes as a tool to optimize the use of waste from rice cultivation and industrial processing. Renewable Energy, v. 111, p. 116-123, 2017).

[013] Also, the article by Anna Brunerova and Milan Brozek, entitled “Is it advantageous to reuse fruit waste biomass from processing of grapevine (vitis vinifera l.) For briquette production? ', Published on May 25, 2017, describes the process of obtaining briquettes from wine production residue, consisting of peel, pulp and grape seeds. This type of starting material has a high homogeneity, which is not observed in solid urban waste, composed mainly of

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5/26 household waste. In order to make the material suitable for briquetting, the material was dried in an oven with air recirculation (BRUNEROVA, A .; BROZEK, M. Is it advantageous to reuse fruit waste biomass from processing of grapevine (Vitis vinifera L.) for briquette production? Engineering for Rural Development, v. 24.26.05.2017, p. 555-560, 2017).

[014] The drying techniques used in the aforementioned documents are not suitable for treating solid urban waste, as they do not allow the collection and / or treatment of residual air, leachate or generated vapors, which leads to potential air contamination. , aquifers and soils.

[015] Patent document CN106675996, entitled “Dry-wet anaerobic coupling processing system and method for organic waste”, priority date 12/30/2016, describes a system for treating MSW through biological processes, with generation of biogas. The biogas obtained is used to provide the thermal energy needed to dry the waste.

[016] Patent document JP2002151131, entitled “Power generation and waste treatment system”, priority date 05/24/2002, describes a system for treating organic waste where a waste fermentation tank produces methane to be used as fuel in processes of steam generation, gasification of residues and cogeneration of electric energy, in the plant itself.

[017] Similarly, patent document US8043505, entitled “Treatment equipment of organic waste and treatment method”, priority date 05/02/2009, describes an apparatus and the process for treating organic waste. In the protected method, the dehydration of the mass of waste is followed by distillation of the generated gases, which will be

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6/26 used in the fermentation of the liquid mass resulting also from dehydration. With the fermentation of the liquid mass, methane is generated for energy generation, used internally in the waste dehydration process.

[018] The abovementioned technologies differ from the technology claimed in this patent application, since biological processes are used for drying and densifying MSW, such as the fermentative processes used to generate methane. The necessary control when using biological processes makes it difficult to install treatment units in remote locations with few resources, which is the reality of several Brazilian municipalities.

[019] Patent document JP2001311513 “Method for drying and treating waste and device for drying and treating raw waste”, priority date April 28, 2000, describes a technology for dewatering MSW by external heating of a rotating drum using combustible gas or electric heating. The gases generated inside the cylinder are sent to the heating chamber of the rotating cylinder to treat odorous gases. The final objective of the process described in the document is the use of dehydrated waste for composting together with waste from tree pruning, with the final product obtained being used as a biofertilizer. The exhaust air from the dehydration chamber is sent to a furnace to treat odorous gases. The technology does not provide, in the dehydration process, direct contact of the heated air with the MSW mass, thus, it is necessary to agitate the residues during heating. The rotating cylinder is heated by the combustion gases, thus diverging from the process described in the present patent application.

[020] Patent document CN102604710, entitled “Device and method for preparing derived fuel using waste

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7/26 urban ”, priority date 10 April 2012, describes a process for obtaining fuel through the dehydration of urban waste. In the described process it is necessary to manually sort the waste in addition to a sorting of metals and, still, two drying steps are necessary. After obtaining the material, the remaining liquid and gaseous waste must be sent to another station to be treated. Therefore, the process has too many steps compared to the process described in the present patent application.

[021] In the process proposed in the present invention, the heated air that enters the dehydration chamber is forced to make direct contact with the solid waste to be treated. In the state of the art, there are no records of the use of decks installed on floors of dehydration chambers to favor the uniform circulation of hot air inside the chamber.

[022] Furthermore, these solid urban residues, after the dehydration stage, may or may not undergo a comminution stage, and may also be mixed with urban pruning residues or wood chips. The temperature of the heated air used to dehydrate the waste is such that it allows drying in a single step, but at the same time it is below the range of potential risk for formation of dioxins and furans. The air removed from the dehydration chamber, containing the extracted moisture, is subjected to a condensation process by direct contact, in a gas washing tower, to reduce moisture and condensables.

[023] The air flow from the washing tower is directed to the furnace to be used as an oxidizer in a fixed chamber. Thus, the same furnace is used for indirect heating of the air flow to be used in the dehydration of solid urban waste, and for post-burning and oxidative destruction of odorous compounds released in the drying process.

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8/26 [024] The gas washing tower inserted between the dehydration chamber and the furnace operates at an appropriate temperature to promote the condensation and removal of moisture present in the air flow, keeping the vapor in a dew point. The reduction of moisture in the oxidizer favors the operating conditions of the furnace, optimizing combustion and reducing energy demand and fuel consumption.

[025] The dehydrated residue obtained in the present process can be sent for combustion in mixture with biomass of forest origin, previously submitted or not to a stage of mechanical densification (briquetting or pelletizing).

[026] The proposed technology presents a series of differentials in relation to existing technologies in the state of the art. The process allows the reduction of mass, volume and elimination of leachate formed during the storage and disposal of solid urban waste, thus providing environmental security in relation to the contamination of aquifers and soils. Also, the reduction of humidity through the dehydration process by transferring heat from the hot air to the waste mass allows the storage of the waste mass without biological decomposition or leachate generation. If dehydrated below a certain value, with a humidity limit of less than 20%, and if protected against rehydration by adequate storage, biodegradability will be restricted, eliminating the formation of greenhouse gases (methane) and odors. The process described here contemplates the reduction of waste moisture to a limit below 12%.

[027] From the process claimed, it is possible to produce a fuel derived from solid urban waste with the use of the new energy modal proposed in clinker furnaces, thermoelectric, among others, that is, in units located in distant locations from the plant. waste treatment. Existing technologies applied to

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9/26 treatment of solid urban waste, whether from grounding or heat treatment, allows, when foreseen, the energy use only in the waste treatment / disposal sites, since the waste cannot be stored and transported over long distances, for being leachate and biologically active generators.

[028] The pleaded process also foresees, without any sorting of residues, the use of organic materials of biogenic origin, which have a high moisture content, bad odor, leachate and percolate, such as food scraps, fruit peels and vegetables, etc. This type of material corresponds to an expressive fraction present in urban solid waste in Brazil.

[029] The process also makes it possible to use biomass from urban pruning, as well as residues from wood processing and agro-industrial residues as fuel to feed the dehydration system furnace. Still, the use of the same furnace for heating the air flow to be used in the dehydration of solid urban waste as a post-burning system and oxidative destruction of odorous compounds released in the drying process, allows energy savings in the treatment of gases and control of odors.

[030] Finally, the claimed process provides for the elimination of vectors and pathogens in solid urban waste provided by the thermal treatment of the material and minimization of the risk of formation of dangerous atmospheric pollutants and emissions of polluting gases in the thermal treatment, due to the mild thermal process. to which solid urban waste is submitted. The control of air pollutants in the treatment process described here is simple and effective.

[031] The process proposed in the present patent application is a dehydration method with an odor control system and elimination of biodegradability and leachate formation capacity, that is, no

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10/26 is not only a method for obtaining dehydrated material for briquetting or pelletizing, but also a method of treating waste to allow its storage and transportation to energy recovery sites far from the waste treatment plant.

BRIEF DESCRIPTION OF THE FIGURES [032] Figure 1 (a) shows a top view of the device for covering the floor of the dehydration chamber, in which it is possible to see the openings (5) and the platform surface (4). Figure 1 (b) shows a perpendicular section in the transverse direction of the platform, in which its main constituent elements are shown: dehydration chamber floor (1), platform support structure (2), air circulation spaces ( 3), platform surface (4), openings (5) and the platform (6).

[033] Figure 2 is a schematic representation of the heat exchange between the combustion gases and the air in the heater.

[034] Figure 3 is the flow chart of the waste treatment process proposed in the present invention, including the parts of the device and all optional steps. (1) is the floor of the dehydration chamber (7), (8) is the flow of heated air that leaves the heat exchanger (10) and enters the dehydration chamber (7), (9) is a washing tower gas, (10) is a heat exchanger, (11) is the gas washing solution reservoir, (12) is the air heating furnace, (13) is another gas washing tower, (14) they are exhaust fans, (15) they are motor pumps, (16) it is a chimney, (17) it is the flow of gases and vapors generated in the dehydration chamber (7), (18) it is the flow of washing solution that comes out of the washing tower (9) and goes to the reservoir (11), (19) is the flow of gases remaining from the condensation obtained in (9), (20) is the flow of exhaust gases from the air heating furnace ( 12), (21) is the flow of washing solution that leaves the washing tower (13) and goes to the reservoir

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11/26 (11), (22) is the treatment, use or disposal of the liquid effluent generated by the condensation process according to environmental legislation, (23) is the discharge of the dehydrated material from the dehydration chamber, (24) is the dehydrated material discharged, (25) is the comminution of waste before entering the dehydration chamber, and (26) is atmospheric air at room temperature that enters the heat exchanger (10).

DETAILED TECHNOLOGY DESCRIPTION [035] The present technology refers to a process of dehydration and densification of waste. The process is an alternative for the treatment of solid urban waste that is currently, in most cases, stored in a landfill, leading to immeasurable environmental damage. In addition to being a waste treatment process, the claimed method also allows obtaining combustible material. The invention also relates to a device containing a platform to cover the floor of the dehydration chamber.

[036] The dehydration and densification process of residues of the present invention (Figure 3) follows the following steps:

a) Place the waste in the dehydration chamber (7);

b) Inject in the dehydration chamber (7) a heated air flow (8), between 100 ° C and 245 ° C, after passing through a heat exchanger (10), and the air must flow through the dehydration chamber ( 7);

c) Route the gases and vapors (17) generated in the dehydration chamber (7), in step “b”, to a gas washing device (9) in which the operating temperature is equal to the water dew point, so that the water vapor condenses and mixes with the gas washing solution, separating it from the remaining washed gases;

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d) Keep the mixture of washing solution and condensed steam obtained in “c” in recirculation (18) with a gas washing solution reservoir (11) at a temperature below 40 ° C;

e) Route the remaining condensation gases obtained in “c” (19) for burning as an oxidizer in the air heating furnace (12);

f) Forward the exhaust gases (20), coming from the air heating furnace (12), for treatment through absorption in a gas washing device (13);

g) Keep the mixture of washing solution and condensed steam (21) obtained in “f” in recirculation with a reservoir of gas washing solution (11) at a temperature below 40 ° C;

h) Drain the gas washing solution from the reservoir (11) and treat, use or dispose of the liquid effluent generated by the condensation process (22) according to environmental legislation;

i) Block the heated air flow (8) to cool the dehydrated material in the chamber (7);

j) Unload the dehydrated material (24) after cooling.

[037] The waste from step “a” is preferably solid urban waste, without any prior sorting. Furthermore, the residues can be comminuted (25) before being placed in the dehydration chamber (7). In step “a”, there may or may not be a mixture of residues with biomass (pruning remains, firewood, wood chips). In step “c” the gas washing solution must operate in a closed circuit, passing through the washers (9 and 13) with return to the recirculation reservoir (11). In step “b”, the time that the residues remain in contact with the heated air is, preferably, 12 hours. The cooling of step “i” lasts, preferably 6 hours.

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13/26 [038] The material obtained in step “i” (24) can be sent to briquetting, with optional milling, screening and mixing steps with biomass before compaction. For briquetting the material must have a humidity of less than 12% and a grain size of less than 5 mm.

[039] The furnace (12) may be fed with various types of biomass, pruning remains, firewood, wood chips, agricultural and agro-industrial waste, among others. The flow of gases will have its movement provided mechanically by exhaust fans (14), while the flow of the gas washing solution will be assisted by motor-pump sets (15). The exhaust gases from the washing tower will be released into the atmosphere through a chimney (16).

[040] The dehydration chamber is equipped with a platform (Figure 1) that allows the passage of the heated air flow through its structure. The platform is positioned on the floor of the dehydration chamber (1) forming a platform (6) elevated in relation to the level of the floor that rests on the support structure of the platform (2). The platform is built in order to allow the heated air flow between the floor and the platform (6) through the air circulation spaces (3), this flow is distributed over the entire surface of the platform through openings (5) , allowing the heated air to circulate evenly inside the dehydration chamber, favoring the dehydration of the MSW that is distributed on the surface of the platform (4).

[041] The present technology can be better understood through the following non-limiting examples.

Example 1 - Material and process characteristics [042] A prototype is designed, as an example of a module that can be replicated. The plant is intended for the thermal treatment of solid urban waste - MSW.

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14/26 [043] The nominal capacity of the plant prototype is 7.5 tons of MSW per day. The gravimetric composition of MSW found is generally the one described in Table 1. The following characteristics were considered for the material to be processed:

· Specific mass: 150 to 300 kg / m ³ (without compaction) · Humidity: 50% (wet basis) · Specific heat: 3.46 kJ / (kg.K) = 0.828 kcal / kg ° C

Table 1 - Gravimetric composition of solid urban waste

COMPONENT % (Dry base) Organic matter 51.4 Steel 2.3 Aluminum 0.6 Paper / Cardboard 13.1 Plastic 13.5 Glass 2.4 Others 16.7

[044] The MSW thermal treatment plant was dimensioned considering the following characteristics for the process and equipment:

· Nominal processing capacity: 7,500 kg of MSW per cycle · Dehydration reactor volume: 60.0 m3 · Number of dehydration reactors: 1 · Number of cycles per day: 1 cycle / day (one for each reactor) [045 ] The dehydration heat treatment process applied to MSW generates a product in the form of dehydrated material. Batch operation was designed for the waste dehydration process (MSW), using a reactor operating in cycles composed of the following

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15/26 sequence: loading, heating, dehydration, cooling and discharge, cleaning.

[046] The expected times for the operational cycle of the dehydration process are shown in Table 2 below.

Table 2 - Operational Cycle - Dehydration Process

STAGE PERIOD (h) Reactor loading 1.0 Heating 3.0 Dehydration 12.0 Cooling 6.0 Unloading the reactor 1.0 Reactor cleaning 1.0 Complete cycle 24.0

[047] The process of thermal treatment of MSW by dehydration begins with the receipt of waste. For processing, the residues must be weighed prior to the reactor supply in order to dimension the process load and verify the loss of mass that occurred after the treatment.

[048] Waste for treatment must be subjected to a comminution process and discharged neatly into the dehydration chamber, using a mechanical loader. It may or may not occur at this stage, the mixing of waste with biomass. Thereafter, the heat treatment process itself begins. The process, carried out in batches, uses a direct heating dehydration chamber by means of heated air flow, promoting the dehydration of MSW at temperatures varying between 245 ° C in the ditch at the entrance of the dehydration chamber and 100 ° C at the exit of the dehydration chamber. dehydration.

[049] During the dehydration process, phase changes occur that result in the removal of moisture from the MSW, releasing gases and vapors.

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As a result, the process causes the reduction of humidity, disinfection of residues, reduction of mass and volume of the processed material.

[050] The hot air must flow through the dehydration chamber, which will keep the temperature at an appropriate level for the development of the process.

[051] At the end of this stage, developed inside the dehydration chamber, the product obtained will be presented in the form of dehydrated material to be subjected to a cooling step in the chamber itself, by blocking the heated air flow.

[052] The gases and vapors generated in the dehydration chamber must be sent to the gas absorption / condensation system. The gas washing solution must operate in a closed circuit, and must pass through the washers with return to the recirculation reservoir. The gas washing solution in the reservoir must be drained, and the liquid effluent generated by the condensation process must be properly disposed of, in accordance with environmental legislation.

[053] The exhaust gases, from the combustion furnace of the gases from dehydration and combustion of biomass, receive treatment through absorption in a gas washing tower.

[054] After the discharge of the dehydrated material, it can be subjected to grinding, sieving, and after the optional mixing with biomass, being with suitable granulometry and humidity, the material can be sent to a briquetting process.

Example 2 - atmospheric emissions from the process [055] To estimate the flow of gases generated by the MSW Heat Treatment System, generation can be divided into two distinct phases, namely the gases and vapors generated by the process inside the chamber dehydration and gases generated by the combustion of biomass

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17/26 to be used as fuel, which should happen inside the gas afterburning furnace.

[056] The gases and vapors from the dehydration process will be sent to a washing / condensation tower. After pretreatment, the gases will be sent to a post-burn zone in a furnace, then from there to a gas washing tower with subsequent release into the atmosphere through a chimney.

Example 3 - Sizing of system units [057] Dehydration chamber - Flow of vapors generated by the dehydration process. For the flow calculation, it was assumed that the condition of the dehydration chamber was loaded to its maximum capacity (batch / intermittent flow), with the release of vapors during a processing cycle.

· Number of dehydration chambers: 1 · Dehydration chamber volume: 60,000 L · Maximum chamber load volume per cycle: 50,000 L · Dehydration period: 12.0 h [058] Considering the specific mass of USW 150 kg / m ³ , we have:

· Total weight per batch: 150kg / m3 x 50m3 = 7,500kg processed per cycle.

· Considering dehydration from U = 50% to U = 10% · Mass of water in the wet residue: 1 _1U = 1 χι _π = 0 ₍ 5χ 7,500 = 3.7501 1 · Mass of solids in the wet residue: 1 ₁ = 1 ₁₁ - 1 ₁₁₁ = 7,500 3,750 = 3,7501 1 · Mass of water in the dehydrated residue: 1 ₁₁₁ = 1 ^ 1/11 - 11 = 3,750 χ 0.1 / (1 - 0.1) = 416.711 · Evaporated water mass: 1 _H = 1 ₁₁₁ - 1 ₁₁₁ = 3,750 - 416.7 = 3,333.31 1

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18/26 · Mass flow of vapors: 1 ₁ = 3,333.3i 1 / 12.01312 = 1277.811 / 0 [059] Dehydration chamber - Heat flow required for heating MSW. Considering the heating of the MSW from Tf = 25 ° C to Tq = 99.1 ° C in a period t = 3.0h and with the specific heat Cp = 0.828kcal / kg ° C, we have:

¹ 11 ¹ 1 ⁽¹ 1 1 = ---------- 7.5001 1 x 0.828 ¹¹ ^ 199.1 - 251 ° 1 ° 1

300 = 153.3871 11 1/0 [060] Considering the coefficient of heat loss in the reactor 1 = 5%, the total heat to be supplied will be:

153.387 = -— ^ - = ------— = 161.4601111 / 0 ¹ (1 - 1) (1 - 0.05) ¹ [061] Dehydration chamber - Heat flow required for dewatering the MSW. With the dehydration of MSW developing at P = 1.0kgf / cm ² and T = 99.1 ° C, we have enthalpy of saturated liquid 1 ₁ = 99.1kcal / kg and enthalpy of saturated steam 1 ₁ = 638.5kcal / kg, so the required heat will be:

11 = 1 110 ₁ - 0.1 = 277.811 / 01638.5 - 99.1u 111/11 = 149.8451111 / 0 [062] Considering the coefficient of heat loss in the dehydration chamber 1 = 5%, the total heat to be provided will be:

Π ¹¹ = (1 - 1) ' 149,845 - --------— = 157.7321 11 1/0 (1 - 0.05)

[063] Dehydration chamber - Hot air flow required for the dehydration process. Being:

· Air inlet temperature: 245 ° C · Air outlet temperature: 110 ° C · Specific air heat: 0.240 kcal / kg ° C

- 157,732

0.24 x 1110 - 2451

4.86811 / 0

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19/26 [064] Furnace / after burning - Biomass combustion. Based on the characteristics of the fuel used to operate the MSW dehydration process and the furnace's energy demand for maintaining the post-burn temperature, the consumption of wood chips by the plant was determined using the AComb 5 software from IPT. Table 3 presents these data.

Table 3 - Plant furnace fuel data *

Fuel Moisture (%) PCS (kcal.k g ^-1 ) PCI (kcal.k g-1) Flow (kg.h ^{- 1} ) Temperatu ra (° C) Specific heat (kcal.kg ^{- 1} .K ^-1 ) Chips 40.0 3542 3127 345.8 25 0.2249 wood

[065] The combustion air and flue gas data were also determined using the AComb 5 software, as shown:

o Combustion air:

· Ii 11 nu i ii ffli ffli ii ui ffli ffli: fflil? L = E435,91l% [* · ii _ii = 5106,5ii / 0ii ii · i ^ & aOHi 1 _{1 ffli} & ffl, 24327liii í / iii ^ ii) i _ii &

a, 116Qli / i ³ Hi i) · ii ii çãiffli lii ii iiiíi ii: li / i = 14.77® i / ii [066] Considering the adjustment of the adiabatic flame temperature to 765 ° C, depending on the furnace requirement, with the temperature required for post-firing.

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20/26 [067] Combustion gases (wet gases). For the calculations referring to the combustion gases, the mass flow rate of the fuel presented in Table 3 and the calculations for the combustion air were considered.

· Íii i iii ii ii 01 ii i ánu 01 0011 1: 1 = 76501 · iii 11111111011011110101 (110101111101: 11 = 75001 · i 1 = 5,452.311 / 0 (ii) · 1 ₁ = 0.333841 1/1 ¹ [ (ii) (i 0 = [750 ° i) · 1 ₁₁ = 0.270330111 / 111 [(11) [(i 0 = [750 ° i) · 0 = 235.251 11 i / ii [(ii) (i 0 = [750 ° i) · i = ₁ ³ 16096.01 / 0 (i = 0 [° I 750) [068] furnace / post burn. - Volume after the burning furnace whereas the minimum time of permanence in the furnace gas i = 1.0 seconds, the volumetric requirement will be:

130 i = ixi = 16,096 — x 1,01 x ----- = 4,471 3 ¹ 036001 · Internal dimensions of the furnace · Length: 1.60 m · Width: 1.80 m · Height: 1.80 m [069] Furnace / after burning - Air heater. The combustion gases leaving the furnace (750 ° C) will be sent to the air heater, so that the heat exchange with the MSW dehydration air occurs, as shown in Figure 2.

[070] The energy balance in the heater allows to estimate the outlet temperature of the hot gases.

11 0 _η φ _Η Β 011) 1 ^ [3 11 ffli 1 ^ 11 1 & 3 _n )

5,452.3 x [0.27033 [(750 [-0 „) [= [4,868.0 x 0.24327 (250 - 25)

1,473.9t? X (750E-0 „) & 266,453.6

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111 0 = 17501? - 180.8 à η 1569.2131 [071] With the heat exchanged and the inlet and outlet temperatures of the gases and the heated air, the required exchange surface for the heater working with parallel currents can be estimated .

113 = 0 1311 311 11

0 = 1266.4540111 / 0

I 0 = 1300/1 ² ° 1 0 = 125.8130111 / 01 ^2o 1 ¹¹¹¹ = ^(Δ1 1 11 ^-Δ1 1 11 ^{) / 11} (Δ1 11 ^{/ Δ1} 1 „) = ((750 - 25) - (569- 250)) / 11 ((750 - 25) / (569-250))

II 110 = 17251-13191/01 (7251/1319) 11110 = 14-94.5131

0 = [266.454 / (25.813 x 494.5) à | 1 0 = Ε20.90 ~ [072] Condensation system - dehydration gases. This system will be responsible for the condensation of the gases generated in the dehydration process. The use of a system consisting of 01 (one) direct contact system of the “hydrojet” washer type is foreseen.

· Gas washer design parameters · Nominal gas flow: Q = 5,850 m ³ / h · Number of ejector channels: 2 [073] Flow of gas washing solution. The gas washing liquid used will be water. The total flow repressed by the pump will be 30 m3 / h for the nominal flow. So for the gas flow of 5,850 m3 / h the liquid / gas ratio of the washer will be:

30m ³ H2O _ 5.1m ³ H2O

5.850m ³ gas 1 .OOOmFgás [074] Condensation system - Lift of gas washing solution.

· Liquid to be repressed: gas washing solution · Flow: 30 m3 / h

Petition 870180015625, of 27/02/2018, p. 36/47

22/26 · Centrifugal motor pump.

· Geometrical difference: 5 m · Straight pipe length: 20 m · Carbon steel pipe [075] Pipe diameters - suction and discharge · Economic diameter: D _e = 1.0730 / 3600 = 0.091m · Nominal suction diameter: D = 4 = 101.6 mm · Nominal discharge diameter: D = 3 = 76.2 mm [076] Flow speeds

4 x 0.00833. V _S = --- „„, ₂ = 1,027 m / s Suction: ^S π x 0.1016 ² 4 x 0.00833 _QO . V _R = --—— y = 1.827m / s Repression: ^R π x 0.0762 ²

· Head Losses 0 = 3 - (Carbon steel) [077] According to the Hazen-Williams formula, head loss due to resistance along the pipe is calculated:

Q = 0.2785 .D .C ^{2, 63.} J ⁰ , ⁵⁴ [078] Where: Q = flow (m ³ / s); D = pipe diameter (m); C = 100 (for carbon steel); J = loss of unit pressure, per meter of pipe (m / m).

[079] Thus, we have:

0.00833 = 0.2785 .100. (0.0762) ² , ⁶³ .J ⁰ , ⁵⁴ [080] Where: J = 0.083 m / m.

[081] Thus, with L = 20 m, the head loss in the straight section is (H _R1 ) = 1.66 m. [082] Assuming that the localized head losses are 5% of the head loss along the pipeline, we have:

Localized Head Losses = H _R2 = 1.66 x 0.05 = 0.08 m [083] Thus, the head will be:

Hman = H0 + Hr1 + Hr ₂ + (nozzle pres)

Petition 870180015625, of 27/02/2018, p. 37/47

23/26

H _man = 5 + 1.66 + 0.08 + 15 = 21.74 @ 22mca

H _man = 22mca (adopted) [084] Motor-pump set · Pump: Centrifugal · For H _man = 22mca and flow rate = 30 m7h, we have:

· Motor: Electric

1000 x 22 x 30/3600 x 0.55

4.89 CV [085] Considering a safety margin of 25% and the powers of the existing commercial engines, we have:

Ninst. = 4.89x 1.25 = 6.11 CV N _iret = 7.5 CV [086] Absorption system by direct contact - combustion furnace gases. This system will be responsible for the treatment of the gases generated in the afterburning furnace. The system consists of 01 (one) washer.

[087] Gas washer design parameters · Nominal gas flow: Q = 16,096 m ³ / h · Number of ejector channels: 4 [088] Gas washing solution flow [089] The gas washing liquid used it will be water. The total flow repressed by the pump must meet the washer and will be 60 m3 / h. So for the gas flow of 16,096 m3 / h the liquid / gas ratio of the washer will be:

_ 60m ³ H2O 3.7 m ³ H2O

16,096m3gas 1,000m3gas [090] Condensation system - Lift of gas washing solution.

· Liquid to be repressed: gas washing solution · Flow: 60 m3 / h

Petition 870180015625, of 27/02/2018, p. 38/47

24/26 · Centrifugal motor pump.

· Geometrical difference: 5 m · Straight pipe length: 20 m · Carbon steel pipe · Reservoir volume: 30 m ³ [091] Pipe diameters - suction and discharge · Economic diameter: D _e = 1.0 ^ 60 / 3600 = 0.129 m · Nominal suction diameter: D = 5 = 127.0 mm · Nominal discharge diameter: D = 4 = 101.6 mm [092] Flow velocities

4 x 0.0167 yo-yo / V _S = ---------- = 1.318 m / s Suction: ^S px 0.1270 ² Repression: 4 x 0.0167 _onc,, V _R = ---------- = 2.056 m / s ^R px 0.1016 ²

· Head Losses 0 = 4- (Carbon steel) [093] According to the Hazen-Williams formula, head loss due to resistance along the pipe is calculated:

Q = 0.2785 .C .D ^{2 '63} . J ^{0 '54} [094] Where: Q = flow rate (m ³ / s); D = pipe diameter (m); C = 100 (for carbon steel); J = loss of unit pressure, per meter of pipe (m / m).

[095] Thus, we have:

0.0167 = 0.2785 .100. (0.1016) ^{2 '63} .J ⁰ ' ⁵⁴ [096] J = 0.074 m / m.

[097] Thus, with L = 20 m, the head loss in the straight section is (H _R1 ) = 1.48 m. [098] Assuming that the localized head losses are 5% of the head loss along the pipeline, we have:

Localized Head Losses = H _R2 = 1.48 x 0.05 = 0.074 m [099] Thus, the head will be:

Petition 870180015625, of 27/02/2018, p. 39/47

25/26

Hman = Ho + H _R1 + Hr2 + (nozzle pres)

H _man = 5 + 1.48 + 0.074 + 15 = 21.554 @ 22mca

H _man = 22mca (adopted) [0100] Motor-pump set · Pump: Centrifugal · For H _man = 22mca and flow = 60 m7h, we have:

· Motor: Electric

1000 x 22 x 60/3600 x 0.5

9.78 CV [0101] Considering a safety margin of 20% and the powers of the existing commercial engines, we have:

N _inst . = 9.78x 1.20 = 11.7 CV

Ninst = 15.0 CV [0102] Gas pipe diameters - Dehydration chamber / Dehydration gas washer / Furnace · Gas flow: 5,850 m ³ / h · Speed: 15 m / s

4x 5,850 / 3600 i x 15

0.371i · Diameter adopted: 380 mm [0103] Gas pipe diameters - Flue gas furnace / scrubber / Chimney · Gas flow: 16,096 m3 / h · Speed: 22 m / s

4xi 4x 16,096 / 3600 i = i ------ = i ------------------- = 0,509i i x i i x 22 · Adopted diameter: 500 mm

Petition 870180015625, of 27/02/2018, p. 40/47

26/26 [0104] Gas pipe diameters - Power required to exhaust the dehydration air. Main features of the system:

· Flow rate: Q = 4,850 m ³ / h · Head loss: DP = 450 mmca · Required power

4,850 x 450

3600 x 75 x 0.6

13.4721 1 [0105] Considering the safety margin of 15% and the powers of the existing commercial engines we have:

N = 13.472 x 1.15 = 15.493 CV N _inst = 15 CV [0106] Gas pipe diameters - Power required for flue gas exhaust. Main features of the system:

· Flow rate: Q = 16,096 m3 / h · Head loss: DP = 100 mmca · Power required

16,096 x 100

3600 x 75 x 0.6 [0107] Considering the safety margin of 20% and the powers of the existing commercial engines we have:

N = 9.936 x 1.20 = 11.923 CV N _inst = 15 CV

Claims (12)

1. DEHYDRATION AND WASTE DENSIFICATION PROCESS CHARACTERIZED BY understanding the following steps: a) Place the waste in the dehydration chamber (7); b) Inject in the dehydration chamber (7) a heated air flow (8), between 100 ° C and 245 ° C, after passing through a heat exchanger (10), and the air must flow through the dehydration chamber ( 7); c) Route the gases and vapors (17) generated in the dehydration chamber (7), in step “b”, to a gas washing device (9) in which the operating temperature is equal to the water dew point, so that the water vapor condenses and mixes with the gas washing solution, separating it from the remaining washed gases; d) Keep the mixture of washing solution and condensed steam obtained in “c” in recirculation (18) with a gas washing solution reservoir (11) at a temperature below 40 ° C; e) Route the remaining condensation gases obtained in “c” (19) for burning as an oxidizer in the air heating furnace (12); f) Forward the exhaust gases (20), coming from the air heating furnace (12), for treatment through absorption in a gas washing device (13); g) Keep the mixture of washing solution and condensed steam (21) obtained in “f” in recirculation with a reservoir of gas washing solution (11) at a temperature below 40 ° C; h) Drain the gas washing solution from the reservoir (11) and treat, use or dispose of the liquid effluent generated by the condensation process (22) according to environmental legislation; Petition 870180015625, of 27/02/2018, p. 42/47 2/3 i) Block the heated air flow (8) to cool the dehydrated material in the chamber (7); j) Unload the dehydrated material (24) after cooling. 2. THE PROCESS, ACCORDING TO CLAIM 1, STEP “a”, CHARACTERIZED BY THE waste being preferably solid urban waste, without any sort of prior sorting. 3. THE PROCESS, ACCORDING TO CLAIM 1, STEP “a”, CHARACTERIZED BY THE RESIDUES that can be comminuted (25) before being placed in the dehydration chamber (7). 4. THE PROCESS, ACCORDING TO CLAIM 1, STEP “a”, CHARACTERIZED BY THE WASTE that can be mixed with biomass, preferably leftovers from pruning, firewood and / or wood chips. 5. THE PROCESS, ACCORDING TO CLAIM 1, STEP “c”, CHARACTERIZED BY the gas washing solution to operate in a closed circuit, and must pass through the washers (9 and 13) with return to the recirculation reservoir (11). 6. THE PROCESS, ACCORDING TO CLAIM 1, STEP b, CHARACTERIZED BY the time that the residues remain in contact with the heated air is, preferably, 12 hours. 7. THE PROCESS, ACCORDING TO CLAIM 1, STEP i, CHARACTERIZED BY THE COOLING, lasts, preferably 6 hours. 8. THE PROCESS, ACCORDING TO CLAIM 1, CHARACTERIZED BY THE material obtained in step “i” (24) can be sent for briquetting. 9. THE PROCESS, ACCORDING TO CLAIMS 1 AND 8, CHARACTERIZED BY THE material sent by the briquetting power Petition 870180015625, of 27/02/2018, p. 43/47 3/3 be subjected to grinding, screening and mixing with biomass steps before compaction. 10. THE PROCESS, ACCORDING TO CLAIMS 1, 8 AND 9, CHARACTERIZED BY THE material to be sent to briquetting, having humidity and granulometry less than 12% and less than 5 mm, respectively. 11. THE PROCESS, ACCORDING TO CLAIMS 1 AND 5, CHARACTERIZED BY THE flow of the gas washing solution between the washing devices and the reservoir to be assisted by pump sets (15). 12. DEVICE FOR COVERING THE FLOOR OF THE DEHYDRATION CHAMBER CHARACTERIZED because it comprises a platform formed by the support structures of the platform (2), air circulation spaces (3), platform surface (4), openings (5) and the platform (6).