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INVENTION
Patent of the Russian Federation RU2249766

METHOD OF COMBUSTION OF SOLID HOUSEHOLD AND OTHER ORGANIC WASTES
AND DEVICE FOR ITS IMPLEMENTATION

The name of the inventor: Kalinin A.V. (RU); Kalinina O.V. (RU); Tikhonov A.V. (RU); Tikhonova EV
The name of the patent holder: Limited Liability Company "Siberian Building Materials and Ecology" LLC "SibstromEco"
Address for correspondence: 660079, г.Красноярск, ул. Sverdlovskaya, 3, LLC "SibstromEco", V.I. Kalinin
Date of commencement of the patent: 2002.05.08

The invention relates to environmentally friendly methods and devices for burning solid domestic and other organic wastes and can be used, in particular, in municipal households for the incineration of waste with guaranteed suppression of harmful substances, including dioxins, with utilization of the heat of combustion of waste and production Commercial lime. The technical result: creation of environmentally favorable process of burning of solid household and other organic wastes with guaranteed suppression of harmful substances, including dioxins, in gas emissions and increase of profitability of incineration plants at the expense of realization of commodity production received during the utilization process. The method for burning solid domestic and other organic waste includes incineration of waste with the supply of preheated air, afterburning of combustion gases, subsequent treatment for binding of HCl, Cl ₂ , HF, passing through the heat exchanger - boiler, gas cleaning. Before entering the furnace for incineration, the waste is separated, the organic part of the waste is crushed to a size of not more than 100 mm, the waste is mixed with air heated to 300-400 ° C, the feed to the cyclone furnace is carried out tangentially with a linear speed of at least 28 m / s, incineration Are carried out at temperatures 1320-1350 ° C, afterburning is carried out in a catalytic afterburner at temperatures of 1300-1500 ° C, treatment for the binding of HCl, Cl ₂ , HF is conducted in a calcined flour calcination chamber to obtain quicklime, before feeding the processed combustion products to the boiler Pass through the air heater, and after the boiler - through a wet gas scrubbing system, and the thermal energy of the boiler is supplied to consumers. An installation for implementing the described method is characterized.

DESCRIPTION OF THE INVENTION

The invention relates to environmentally friendly methods and devices for burning solid domestic and other organic wastes and can be used, in particular, in municipal households for the incineration of waste with guaranteed suppression of harmful substances, including dioxins, with utilization of the heat of combustion of waste and production Commercial lime.

There is a known method for processing garbage at the Moscow Special Plant No. 3 ("Sanitary cleaning and cleaning of populated areas", Handbook, 1990), the main technological equipment for which was supplied by Volund (Denmark). A distinctive feature of this design is the afterburnt rotating drum, installed behind the cascade of inclinedly pushing grate grids, which allows burning in the boiler-aggregate waste of high humidity.

The disadvantage of the method is the thermal processes at the incineration plants due to the presence of a dry ash removal system and, therefore, in order to avoid slagging of the process equipment, run at temperatures of 900 ... 1000 ° C and therefore do not solve the problem of suppressing hazards, in particular, dixins.

Irreversible destruction of thermally persistent organochlorine compounds (dioxins) occurs at temperatures close to 1400 ° C.

A method for processing solid waste in a slag bath is known under the design conditions of melting, whereby the loading of a certain number of necessary fluxes, for example, containing silica (sand, quartz fluxes, etc.), is selected for viscosity and melting point (usually 1300-1500 ° C) Slag composition (RU 2030684 C1, F 23 G 7/00, 10.03.1995). The process is carried out at a controlled oxygen potential (oxidizing conditions), which is specified by the specific oxygen consumption per ton of loading.

Disadvantage of the method: do not take into account the ability of dioxins to a new synthesis at low temperatures. This is particularly facilitated by the conditions typical for the known method of large removal of dust and toxic metal compounds.

A method for the heat treatment and disposal of garbage and household waste in a device that is a vertically disposed shell lined with refractory material is known (RU 2023211 C1, F 23 G 5/00, 15.11.1994). Wastes are loaded from above and go through all the processing stages - drying, pyrolysis, gasification, combustion - in compartments separated from each other by remote-controlled shutters. The gasification process is completed by the formation of a fuel (pyrolysis) gas, which can be sent as fuel to heat power plants.

The technical problem solved in the known invention consists in increasing the efficiency of waste processing associated with the continuous flow of storage, venting, drying, pyrolysis, combustion and ash removal processes in a single sluice monoblock.

Disadvantage of the method - it is necessary to strictly monitor the temperature of the process to prevent caking of coked garbage and waste products on the flaps. For this purpose, the air entering the combustion is moistened, keeping the temperature in the combustion zone no higher than the melting temperature of the ash, and the supply of waste from the zone to the zone is carried out in controlled doses, periodically shaking.

Thus, the involvement of additional thermal operations (pyrolysis, gasification) complicates the process of incineration of waste, increases operating costs, makes the process of waste disposal unprofitable and does not solve problems with the synthesis of dioxins.

The closest analogue is the method for burning solid municipal waste according to RU 2114357 C1, F 23 G 5/00, 27.06.1998 / 1 /.

The known method (1) involves incineration of waste at temperatures above 1340 ° C with the supply of primary air at a temperature of up to 400 ° C, afterburning of gaseous combustion products at temperatures above 850 ° C, subsequent treatment for binding HCl, Cl ₂ , HF, etc., Passing through an electrostatic precipitator into a heat exchanger, which uses a boiler whose heat energy is passed to the consumer.

The disadvantages of the known method are as follows.

Firstly, the inclined-pushing grate (as a rule, from heat-resistant cast iron) is not designed to burn fuel with a temperature greater than 1000 ° C, so the operation of inclined-pushing grates with a temperature higher than 1340 ° C will lead to their rapid wear and tear Out of the furnace.

Secondly, it is well known that the afterburning temperature of 850 ° C does not promote the decomposition of dioxins and furans in combustion products, which indirectly confirm the authors of the known method, establishing after the afterburner another adsorber, where by means of specially prepared lime milk the combustion products are purified, in particular , From hydrogen chloride (a necessary and sufficient component of dioxins and furans).

Thirdly, the use of lime milk in an adsorber (where combustion products with a temperature of 850 ° C arrive) is completely unacceptable for two reasons: first, there will be an almost instantaneous evaporation of the liquid phase of lime milk, accompanied by a sharp drop in the temperature of the combustion products (heat losses of up to 600 Kcal per 1 kg of H ₂ O); Secondly, lime milk is an aqueous suspension of calcium hydroxide at the maximum water: lime ratio of 1: 0.15, so after the conversion of the aqueous component to steam, the amount of solid lime will be so insignificant that the absorption effect will be close to zero.

Fourthly, in the known method an additional energy carrier (gas, fuel oil) is used to stabilize the process, which will lead to a serious increase in the cost of operating costs.

The aim of the invention is to increase the efficiency of the waste incineration process at temperatures above 1300 ° C, to improve the afterburning process of the waste combustion products under catalytic oxidation conditions at temperatures of 1350-1400 ° C, to deepen the decontamination of combustion products by chemisorption of halogens, nitrates, sulfites and other harmful substances On the active surfaces of calcium oxide synthesized by calcination from limestone flour; Full utilization of the internal energy of the waste without involving additional energy resources for the operation of the process.

The object of the invention is achieved due to the fact that in the method of incineration of solid domestic and other organic wastes, incineration of waste with the supply of preheated air, afterburning of combustion gases, subsequent treatment for binding of HCl, Cl ₂ , HF, passing through a heat exchanger - a boiler, gas purification - before entering the furnace for incineration, the waste is separated with the separation of the inorganic part, the organic part of the waste is reduced to a size of not more than 100 mm, the waste is mixed with the air heated to 300-400 ° C, the feed to the cyclone furnace is carried out tangentially at a linear speed of not less than 28 m / s, incineration is carried out at temperatures 1320-1350 ° C, afterburning is carried out in a catalytic afterburner at temperatures of 1300-1500 ° C, treatment for the binding of HCl, Cl ₂ , HF is conducted in a calcareous flour decarbonization chamber to obtain quicklime before Feeding to the boiler, the processed combustion products are passed through the air heater, and after the boiler - through the wet gas cleaning system, and the thermal energy of the boiler is supplied to the consumer.

The apparatus for carrying out the method comprises equipment for separating and grinding waste, a waste bunker, a cyclone furnace with a tangential inlet of a mixture of ground waste and heated air, a catalytic afterburning chamber operating on the principle of a flameless burner, a decarbonization chamber equipped with a hopper and a feeder for limestone flour, Air heater, heat exchanger, wet gas cleaning system.

The essence of the method lies in the fact that before waste is fed to the furnace, the waste is separated with the separation of the inorganic part (metal, glass, ceramics), the organic part of the waste is crushed to a fineness of not more than 100 mm. The shredded waste is fed into a cyclone furnace with a tangential inlet heated to 300- 400 ° C air, the linear velocity of which is not lower than 28 m / s; The resulting combustion products pass through a catalytic afterburner operating on the principle of a flameless burner and a decarbonization chamber where limestone flour (CaCO ₃ ) is sprayed to meet the flow of gases to trap HCl, SO ₂ , NO _x , resulting in thermal exposure to quick lime (CaO ), On the surface of which, as a result of the interaction, in particular with chlorine, CaCl2 crystals are formed, which do not degrade the commercial properties of quicklime.

Thus, in the decarbonation chamber, the secondary formation of dioxins is minimized, up to complete elimination, since it is known that the reactions of their formation take place on the surface of fly ash particles in the presence of chlorine compounds during catalysis by iron and copper compounds.

Then the combustion products pass through the air heater, heating the blast air to 300-400 ° C, and they enter the heat exchanger, from where they are sent to the wet cleaning system, where residual SO ₂ , NO _x and dust are suppressed. Purified gases are discharged into the atmosphere, with the heat energy removed from the heat exchanger circuit and commercial lime being supplied to consumers.

JUSTIFICATION OF THE LIMITS OF THE APPLICABLE OBJECT

The size of the shredding of waste organic matter not more than 100 mm is chosen for reasons of technological expediency, since larger fragments make it difficult to feed waste into the furnace with a tangential input.

The temperature of heated air in the range 300-400 ° C is limited by the technical capabilities of existing air heaters.

The quality of waste combustion in a cyclone is limited by the linear velocity of the blown air mixture with waste: the higher the speed, the higher the combustion quality.

It was experimentally established that at a speed below 28 m / s the percentage of chemical and physical underburning sharply increases, which ultimately leads to the synthesis of dioxins.

Limestone flour (CaCO ₃ ) at temperatures of 1300-1500 ° C is decarbonized almost instantly within a fraction of a second by the reaction:

CaCO ₃ -> CaO + CO2

The essence of the device for carrying out the method is shown in FIG. 1 and FIG.

1 schematically shows a device, a vertical section B-B; FIG. 2 shows a section AA.

The device for burning solid domestic and other organic waste contains a waste hopper 1, channel 2 for the joint supply of crushed waste and heated air, a cyclone furnace 3 with a tangential inlet of a mixture of waste and air, a catalytic afterburner 4 operating on the principle of a flameless burner, a chamber Decarbonization 5, equipped with a hopper 6 and a disk feeder 7 for limestone flour.

In the air heater chamber 8, a metallic air heater 12 is mounted. The fan 10 feeds the heated air through the duct 11 to the hopper with crushed waste.

Example 1 of the practical implementation of the method and apparatus for burning solid domestic and other organic wastes with guaranteed suppression of harmful substances, including dioxins.

For example, the productivity of an incineration plant operating according to the proposed method is 6 tons per hour.

The plant functions as follows.

At the separation stage, inorganic waste (metals, glass, ceramics, etc.) is separated, which is usually about 6%. Typical equipment for magnetic and air separation is used for these operations.

The organic part, after separation consisting of waste paper, food waste, wood, textiles, leather, rubber, plastic, is fed for grinding up to a piece size of not more than 100 mm. Crushing is carried out in typical equipment, for example in gear grinders. Then, by blowing air heated to 300-400 ° C with a speed of at least 28 m / s, a mixture of air and crushed waste is blown into the furnace, where it burns at a temperature of about 1320-1350 ° C.

The resulting combustion products pass through a catalytic afterburner chamber, which is a slotted vertical shaft made of aluminosilicate refractories, operating on the principle of a flameless burner, where heavy hydrocarbons and fragments of soot are burned, resulting in a combustion temperature of 50-70 ° C.

Then the combustion products enter the decarbonisation chamber, which is a hollow vertical shaft, from the bottom upwards, where limestone flour (CaCO ₃ ) is sprayed into the chamber in an amount of 270 kg / h (the estimated amount is 6 tonnes per hour of waste).

The resulting quicklime (CaO) in an amount of about 155 kg / h catches chlorine in the combustion products, thus eliminating the possibility of secondary dioxin synthesis.

Neutralized combustion products pass the air heater chamber, heating the blast air, and enter the heat exchanger, which can be a steam or hot water boiler.

After the heat exchanger, the exhaust gases are subjected to final wet scrubbing to neutralize residual SO ₂ , NO _x and dust.

As a wet gas scrubber, a disintegrator or a wet scrubber can be used.

Spent, neutralized and purified combustion products are released into the atmosphere.

Received as a result of the implementation of the method of burning solid domestic and other organic wastes with guaranteed suppression of harmful substances, including dioxins, commercial products - heat energy in an amount of not less than 12.0 Gcal / h and quicklime in an amount up to 150 kg / h - released Consumers, which pays for the money spent.

EXAMPLE 2 Practical realization of the claimed method.

Suppose that the productivity of a waste incineration plant (MSW) for solid household waste (MSW) is 10 ton / h. The MSW entering the MSZ has the following morphological composition (% by mass):

- paper - 35.1;

- food waste - 18.5;

- wood - 2,2;

- Textiles - 7,6;

- skin - 2,8;

- rubber - 3,3;

- plastics - 8,7;

- glass, concrete, ceramics - 10,3;

- Metals - 11.5.

The average calculated moisture of solid waste is 32%.

At the separation stage, inorganic wastes (glass, concrete, ceramics, metals) are separated, totaling 21.8%. For this purpose, magnetic, mechanical, air and partially manual separation equipment is used.

The organic part after the selection of the inorganic is in the wet state:

The same in absolutely dry condition:

The average elemental composition of absolutely dry solid waste for the case under consideration: C - 44.0%, H - 5.2%; О - 28,5%; S = 0.1%; Cl: 0.3%; N, 4.4%; Ash - 17.5%.

Consequently, 5.32 tons of absolutely dry solid waste contain: C - 2.34 tons; Н - 0,28 t; О - 1,52 t; S - 0.0053 t; Cl - 0.016 t; N - 0,23 t; Ash - 0.93 t.

Organic part of solid waste with a humidity of 32% is subjected to grinding to fragments with dimensions not exceeding 100 mm. Crushing is carried out, for example, in gear grinders. Further, the shredded organic waste is blown into the cyclone by a stream of air heated to 300-400 ° C, while the jet velocity is not lower than 28 m / s. In a cyclone furnace combustion of solid waste takes place.

We calculate the thermotechnical and physicochemical parameters of this process.

For the burning of 5.32 tons of absolutely dry solid waste, an amount of air is required, determined by the stoichiometric ratio of the oxidation reactions:

C + O ₂ = CO ₂

H ₂ + 0.5 O ₂ = H ₂ O

S ₂ + ₂ O ₂ = ₂ SO ₂

Or equivalent mass quantities:

2.34 t C + 6.25 t O ₂ = 8.79 t CO ₂

0.28 t H ₂ + 2.24 t O ₂ = 2.52 t H ₂ O

0.0053 t S + 0.0053 t O ₂ = 0.01 t SO ₂

Total oxygen is 8.4953 tons. With an excess of oxidizer = 1,4 the need for oxygen will be 11.89 tons. We subtract the oxygen present in the MSW:

11.89-1.52 = 10.37 tons.

The amount of air required for blasting is found from the calculation of the content of 0.233 kg of oxygen in 1 kg of air:

B = 10.37 / 0.233 = 44.5 t / h

The heat content of 44.5 tons of air at a temperature of 300-400 ° C is equal to 3.34-4.54 Gcal.

Thus, for the burning of 5.32 t / h of an absolutely dry organic solid waste substance, 44.5 t / h of air is required, thus generating 49.82 t / h of combustion products of composition:

СО ₂ - 8.79 t

H ₂ O - 2.52 t

SO ₂ - 0.01 t

O ₂ - 1.88 t

Cl - 0.016 t

N - 35.674 t

Ash - 0.93 t

If the humidity of solid waste is 32%, then the waste contains, in addition to the absolutely dry part, 2.5 tons of physical water, so the total amount of combustion products will be 52.32 tons / hour with the following content of compounds:

СО ₂ - 8.79 t 24.6%

H ₂ O - 5.02 t 14.1%

SO ₂ - 0.01 t 0.028%

O ₂ - 1.88 t 5.27%

Cl-0.016 t 0.045%

N - 35,674 tons 53.36%

Ash - 0.93 t 2.6%

As a result of combustion of 2.34 tons of carbon (at its calorific value 8100 kcal / kg), thermal energy will be released in the amount of:

Q _c = 2340 · 8100 = 18954000 kcal

The same with the combustion of hydrogen (with its heating value of 32,400 kcal / kg):

Q _h = 2800 · 32400 = 9072000 kcal

The same with the combustion of sulfur at a calorific value of 2070 kcal / kg:

Q _s = 5.3 · 2070 = 10970 kcal

Total heat generation in the theoretically complete combustion of solid waste is:

Q _total = 18,954,000 + 9072000 + 10970 = 28036970 kcal

Together with the heat content of heated air, the theoretical amount of heat released reaches 32.6 Gcal / h.

The actual amount of released thermal energy depends on mechanical and chemical underfunding and heat loss to the environment. Usually these losses total up to 20%. Therefore, the actual release of thermal energy by burning in a cyclone furnace of the wet organic part of solid waste is:

Q _p = 32.6 Gcal · 0.8 = 26.0 Gcal / h

The temperature of the combustion products at the exit from the cyclone furnace:

26000000 kcal - thermal performance of the furnace,

52320 kg - the amount of combustion products,

0,375 kcal / (kg · deg) - specific heat of combustion products at 1325 ° C.

From the cyclone furnace, the combustion products pass through the channels of the catalytic afterburner chamber, resulting in almost complete oxidation of the products related to chemical underburning, as a result - the heat content of the combustion products grows by 5-6% (1.3-1.6 Gcal / h) , And the temperature increases by 60-70 ° C and reaches 1385-1400 ° C.

Then the combustion products (52320 kg / h) enter the decarbonisation chamber, the vertical shaft, from the bottom up. Toward the stream, limestone flour (CaCO ₃ ) is sprayed in an amount of 2200 kg / h with an average particle diameter of 0.15 mm.

From the practice of calcining limestone (Yu.M. Butt et al. Chemical technology of knitting materials, M .: Higher School, 1980) it is known that the time for the complete dissociation of limestone particles with a particle size of 0.1-0.15 mm at a temperature of 1100-1200 ° C Is about 0.002 min (0.12 s), i.e. Almost immediately, accompanied by a strong loosening of the structure of the formed calcium oxide. During this period, calcium oxide is extremely active in the absorption of halogens, nitrates, and sulfur.

The work of NIISTROMKompozit, Krasnoyarsk, established a functional relationship between the amount of absorbed substances and the fractional composition of limestone flour dissociating at temperatures of 1100-1200 ° C. In particular, for rough calculations, these indicators are as follows:

Absorption of HCl - 12.9 g / kg of CaCO ₃ ,

Absorption of SO ₂ - 11.4 g / kg of CaCO _3.

If in the combustion products the content of Cl is 16 kg and the SO ₂ content is 10 kg (see above), then the required amount of CaCO ₃ to absorb these compounds is:

HCl 16,000 g: 12.9 g / kg = 1240 kg of CaCO ₃ ,

SO ₂ - 10,000 g: 11.4 g / kg = 877 kg of CaCO _3.

Total: 2117 kg of CaCO ₃ , taken as 2200 kg of CaCO _3.

As a result of dissociation of 2,200 kg of CaCO ₃ , an average of 1270 kg of CaO and 930 kg of CO _{2 is} formed. Chemically adsorbed on the surface of CaO, chlorine and sulfur dioxide synthesize respectively CaCl ₂ and CaSO ₄ , the first in an amount of 25 kg, the second in an amount of 17 kg. In total, these impurities in the mass of CaO are not more than 3.3%. These impurities (calcium chloride and gypsum) have a favorable effect on the hardening of lime, so their presence does not worsen, but improves the quality of calcined lime.

To carry out the dissociation of CaCO _3, 425 kcal per kg of carbonate is required, therefore, at dissociation of 2200 kg of CaCO _3, 0.935 Gcal of thermal energy is absorbed and the volume of combustion products increases by 930 kg of CO ₂ (53250 kg).

Neutralization of combustion products in an amount of 53250 kg with a heat content of 25.8 Gcal (costs for dissociation, heat loss with decomposition products, heat loss to the environment are taken into account) are sent to the air heater chamber. The temperature of the combustion products at the inlet to the air heater is:

As a result of heating the air to a temperature of 400 ° C, 1.6 Gcal of thermal energy is expended. Consequently, from the air heater to the steam or hot water boiler will enter 53250 kg of combustion products with an approximate heat content of 24.2 Gcal and a temperature of 1200 ° C.

From the boiler combustion products will leave with a temperature of 150 ° C, so their heat content will be:

53250 · 0.25 · 150 = 1996875 kcal, 2 Gcal were taken.

The amount of thermal energy processed in the boiler is:

24.2-2 = 22.2 Gcal / h.

If the efficiency of the boiler is taken equal to 0.92, then the commercial thermal energy of the boiler will be:

22.2 · 0.92 = 20.4 Gcal / h.

Thus, if the capacity of the waste processing plant according to the claimed method is 10 t / h of solid waste, then after sorting by incineration of the organic part of these wastes with the disinfection of the combustion products, initially in the catalytic afterburner chamber due to temperature increase up to 1400 ° C and further in the decarbonization chamber at the consumption rate Limestone flour 2200 kg / h due to the chemisorption interaction of halogens, nitrates, sulfites, etc. with the active surface of synthesized calcium oxide completely neutralized combustion products, with the output of commercial lime in the amount of 1270 kg / h, and with the passage of neutralized combustion products through Heat exchanger, the output of commercial heat energy reaches 20.4 Gcal / h.

CLAIM

1. A method for burning solid domestic and other organic wastes, comprising incineration of waste with the supply of preheated air, afterburning of combustion gases, subsequent treatment for binding HCl, Cl ₂ , HF, passing through a heat exchanger-boiler, gas purification, characterized in that before feeding In the combustion furnace, the waste is separated, the organic part of the waste is reduced to a size of not more than 100 mm, the waste is mixed with air heated to 300-400 ° C, the feed to the cyclone furnace is carried out tangentially at a linear speed of not less than 28 m / s; Temperatures 1320-1350 ⁰ С, afterburning is carried out in the catalytic afterburner at temperatures of 1300-1500 ° C, the treatment for binding of HCl, Cl ₂ , HF is conducted in the decarbonization chamber of limestone flour to obtain quicklime, before being fed into the boiler, the processed combustion products are passed through Air heater, and after the boiler - through a wet gas scrubbing system, and the thermal energy of the boiler is supplied to consumers.

2. A method according to claim 1, characterized in that an inorganic portion of the waste is separated off during separation.

3. The apparatus for carrying out the method of claim 1, characterized in that it comprises equipment for separation and grinding of waste, a hopper-waste feeder, a cyclone furnace with a tangential inlet of a mixture of ground waste and heated air, a catalytic afterburning chamber operating on the principle of a flameless burner , A decarbonization chamber equipped with a hopper and a feeder for limestone flour, an air heater, a heat exchanger, a wet gas scrubbing system.

4. The device according to claim 3, characterized in that the catalytic afterburner chamber is made of slit of aluminosilicate refractories.

5. Apparatus according to claim 3 or 4, characterized in that the decarbonation chamber of limestone flour is made in the form of a vertical shaft in which hot gases rise from the bottom upward, and limestone flour sprayed in the upper part of the shaft moves from the top down.

print version
Date of publication on February 21, 2007

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