阅读说明：本技术 操作包括捕获烟道气体夹带的灰分的设备的焚烧装置的方法 (Method of operating an incineration plant of a plant comprising capture of flue gas entrained ash ) 是由 约瑟夫·扬·彼得·比尔曼 于 2019-09-16 设计创作，主要内容包括：一种用于对固体燃料的焚烧装置(100)进行操作的方法,所述焚烧装置(100)包括用于将来自烟道气体的灰分进行分离的装置(160),该方法的包括以下步骤：从所述焚烧装置(100)收集源自于包含灰分的烟道气体的灰分沉积物,从而获得所收集的灰分；为了改善所收集的灰分的流动性,该方法包括以下步骤：将包含i)粘土和ii)碳酸钙的粉末状添加剂材料引入到包含灰分的烟道气体中,其中,包含灰分的烟道气体在引入添加剂材料的位置处具有至少700℃的温度,其中,以比率R引入添加剂,该比率R是包含灰分的烟道气体流中的灰分的质量的至少0.1倍。(A method for operating an incineration plant (100) for solid fuel, said incineration plant (100) comprising means (160) for separating ash from flue gases, the method comprising the steps of: collecting ash deposits originating from flue gas comprising ash from the incineration device (100), thereby obtaining collected ash; in order to improve the flowability of the collected ash, the method comprises the steps of: introducing a powdered additive material comprising i) clay and ii) calcium carbonate into a flue gas comprising ash, wherein the flue gas comprising ash has a temperature of at least 700 ℃ at the location of introduction of the additive material, wherein the additive is introduced at a ratio R which is at least 0.1 times the mass of ash in the flue gas stream comprising ash.)

1. A method of operating an incineration device (100), the incineration device (100) comprising:

a chamber (110) for incinerating a solid fuel in the presence of an oxygen-containing gas,

-a flue gas channel (120) for passing flue gas discharged from the chamber (110) to a discharge, wherein the flue gas comprises ash, and

-a device (160) for separating ash from the flue gas into:

-a flue gas having a reduced ash content, and

-ash;

wherein the method comprises the steps of:

-introducing an oxygen-containing gas and a solid fuel into the chamber (110) to burn the solid fuel, thereby producing a stream of flue gas comprising ash,

-capturing ash from the stream of flue gas comprising ash using the apparatus (160), and

-collecting from the incineration device (100) ash deposits originating from the flue gas comprising ash, thereby obtaining collected ash;

wherein the method comprises the steps of: introducing a powdered additive material comprising i) clay and ii) calcium carbonate into the flue gas comprising ash using an injection inlet transverse to the flow of the flue gas comprising ash, wherein the flue gas comprising ash has a temperature of at least 700 ℃ at the location of introduction of the additive material and is introduced upstream of the apparatus (160), wherein powder particles of the powdered additive material comprise particles, each particle comprising a mixture of clay and calcium carbonate, at least 10% by weight relative to calcium carbonate being calcium carbonate in the form of: when characterized by thermogravimetric analysis at a heating rate of 10 ℃ per minute in a nitrogen environment, the calcium carbonate in said form has been completely decomposed when reaching a temperature of 875 ℃;

and wherein the powdered additive material is introduced at a ratio R that is at least 0.1 times the mass of ash in the stream of flue gas containing ash.

2. The process according to claim 1, wherein at least 40% by weight with respect to the calcium carbonate is calcium carbonate in the form of: when characterized by thermogravimetric analysis at a heating rate of 10 ℃ per minute in a nitrogen environment, the form of calcium carbonate has been completely decomposed when reaching a temperature of 875 ℃, more preferably at least 70% by weight with respect to calcium carbonate of the form.

3. A method according to claim 1 or 2, wherein the additive material is introduced using a plurality of injection ports, wherein the number of injection ports is selected such that the amount of flue gas per injection port is at least 10000kg of flue gas per hour.

4. The method according to any one of the preceding claims, wherein the solid fuel is a fuel comprising a material of non-fossil biological origin.

5. A method according to any one of the preceding claims, wherein the additive material is introduced into the flue gas comprising ash, wherein the flue gas comprising ash has a temperature in the range from 875 ℃ to 1050 ℃, and preferably the flue gas comprising ash has a temperature in the range from 900 ℃ to 1000 ℃.

6. A method according to any one of the preceding claims, wherein the amount of additive material introduced is controlled in dependence on the ash content in the flue gas comprising ash.

7. A method according to any one of the preceding claims wherein the powdered additive material is introduced at a ratio R which is 0.2 to 5 times the mass of ash in the stream of flue gas containing ash, preferably the ratio R is a ratio between 0.3 and 2 times the mass of ash in the stream of flue gas containing ash, and most preferably the ratio R is a ratio between 0.4 and 1.2 times the mass of ash in the stream of flue gas containing ash.

8. The method according to any of the preceding claims, wherein the incineration plant (100) is part of a plant further comprising a unit for thermal conversion of paper waste material containing kaolin, wherein the kaolin is thermally treated in a fluidized bed with free space in the presence of an oxygen-containing gas,

wherein the fluidized bed is operated at a temperature between 720 ℃ and 850 ℃, the temperature of the freeboard being 850 ℃ or lower, thereby producing the powdered additive material, which is introduced into the flue gas of the incineration device (100) comprising ash.

9. The method according to any one of the preceding claims, wherein the weight/weight ratio of switchable calcium carbonate to clay is in the range of from 1 to 10, preferably the weight/weight ratio of switchable calcium carbonate to clay is in the range of from 1 to 5, and more preferably the weight/weight ratio of switchable calcium carbonate to clay is in the range of from 1 to 3.

10. The method according to any one of the preceding claims, wherein the water content of the powdered material is less than 0.9% wt./wt.%, preferably the water content of the powdered material is less than 0.5% wt./wt.%.

Technical Field

The invention relates to a method for operating an incineration device, comprising:

a chamber for incinerating a solid fuel in the presence of an oxygen-containing gas,

-a flue gas channel for passing flue gas discharged from the chamber to a discharge, wherein the flue gas contains ash, and

-a plant for separating ash from flue gases into:

-a flue gas having a reduced ash content, and

-ash;

wherein the method comprises the steps of:

-introducing an oxygen-containing gas and a solid fuel into the chamber to incinerate said solid fuel, thereby producing a stream of flue gas comprising ash,

-capturing ash from a stream of flue gas containing ash using the apparatus, and

-collecting ash deposits originating from flue gases containing ash from an incineration device, thereby obtaining collected ash.

Background

It is well known that incineration of solid fuel produces ash (ash). A portion of this ash may remain in the chamber and be collected therefrom. However, minute ash particles (fly ash) may be entrained by the flue gas and may be discharged to the environment. Since this is considered undesirable, it is known to use a device such as a cyclone, an electrostatic filter, a fabric filter or a gravity settler (the part of the discharge channel having an increased cross-sectional area, so that the flow rate is lower to enable particles to settle there). Such equipment must be cleaned.

The problem is that the ash collected from the apparatus, as well as the ash collected from the incineration device, which adheres to the inner surface of the incineration device after the combustion chamber and before the apparatus, has a tendency to form bridges, reducing its tendency to flow. For example, if the incineration device includes a valve or auger for removing the collected ash, the ash may not pass through the valve, or may not enter the auger, or may be less easy and therefore not easily transportable. Furthermore, the collected ash must then be transported by, for example, trucks, and the limited flow capacity allows for longer periods of truck loading.

Disclosure of Invention

It is an object of the present invention to improve the flowability of ash collected from a stream of flue gas.

For this purpose, the method according to the preamble is characterized in that it comprises the following steps: introducing a powdered additive material comprising i) clay and ii) calcium carbonate into an ash-containing flue gas using an injection port transverse to the flow of the ash-containing flue gas, wherein the ash-containing flue gas has a temperature of at least 700 ℃ at the location of introduction of the additive material and is introduced upstream of the apparatus, wherein powder particles of the powdered additive material comprise particles, each particle comprising a mixture of clay and calcium carbonate, at least 10% by weight, relative to the calcium carbonate, of the calcium carbonate being in the form of: when characterized by thermogravimetric analysis at a heating rate of 10 ℃ per minute in a nitrogen environment, the calcium carbonate in said form has been completely decomposed when reaching a temperature of 875 ℃;

and wherein the powdered additive material is introduced at a ratio R that is at least 0.1 times the mass of ash in the stream of flue gas containing ash.

It has been found that the collected ash and additive containing material has a better flow ability. It has also been found that the total amount of particles (ash and additives) that are discharged to the environment through emissions is reduced.

It has been found that not all calcium carbonates are equal. Using thermogravimetric analysis (TGA), calcium carbonate-containing additive materials can be selected that are suitable for reducing bridge formation in the resulting particulate ash material collected from the apparatus.

Distribution of heatAnalysis (TGA) measures the degradation of quality by heating a sample at a particular rate in a particular environment. The measured quality degradation of the additive material can then be attributed to CaCO₃And CO released simultaneously therewith₂. For the claimed invention, the methods described by a.w.coats and j.p.redfern in thermogravimetric analysis; a review, analyze, 1963,88, 906-: 10.1039/AN9638800906 is a standard method.

Background: due to CaCO₃Is different from the molar amount of CaO, so that the CO release can be measured₂The difference in quality due to decomposition. In practice, it can be verified that the measured weight loss is actually due to the evolution of gaseous CO₂And (4) causing. To this end, the gas leaving the outlet of the TGA measurement device is characterised by any suitable method, for example mass spectrometry.

To briefly illustrate the method of Coats et al, the TGA measurement is a ramp from ambient temperature to a typical 1100 ℃ in a nitrogen environment at a ramp rate of 10 ℃ per minute. The weight of the sample is expressed as a percentage of calcium carbonate, where 100% represents unconverted calcium carbonate. Due to CaCO₃Is 100g/mol, CO released on heating the carbonate₂Since the molar amount of (b) is 44g/mol, the remaining mass fraction after decomposition is 56%.

In the art, it is known to use dolomite or limestone as captured SO₂The additive material of (1). It has been found that these additive materials achieve complete decomposition only at higher temperatures and/or increased residence times, which is not satisfactory for practical use, particularly in the case of solid fuels containing non-fossil biological material (plant material) and domestic waste, where the temperature of the flue gas containing ash is generally relatively low.

In the present application, the term "solid fuel" means that the fuel is solid at a temperature of 30 ℃. The chamber into which the fuel is introduced is for example the chamber of a fluidized bed or grate incineration plant. The fuel particles may be relatively small in size (e.g., on the order of millimeters or less) or relatively large in size (e.g., on the order of centimeters or more). The solid fuel is for example biomass, waste from industrial processes or households or mixtures thereof.

The term "powdered material" indicates a material having a particle size of less than 100 μm. These particles have the property of being granular, i.e. the particles typically comprise a large number of smaller particles.

Typically, the additive material is introduced into a flue gas comprising ash, wherein the flue gas comprising ash has a temperature of at least 800 ℃ and less than 1150 ℃. In incineration processes involving a flame, it is preferred to inject the additive material downstream of the flame. The pneumatic injection is usually carried out using air as transport medium, using injection ports oriented transversely to the direction of the flue gas flow, and applying a pneumatic transport medium at a velocity of typically more than 10m/s, more preferably more than 15 m/s. Preferably, the injection is performed using at least one injection lance projecting in the flow of flue gas containing ash.

The residence time of the additive in the flue gas containing ash before reaching the plant is typically at least 1 second, preferably at least 3 seconds, and more preferably at least 5 seconds. Thus, interaction with ash particles is enhanced to improve ash capture.

In the present application, a flue gas comprising ash is a flue gas containing non-gaseous materials. Such non-gaseous materials in the flue gas typically include solids and/or at least partially include molten particles derived from the fuel that, upon cooling, become solid ash. Thus, in the present application, the term "ash" in the term "flue gas containing ash" relates to a non-gaseous material, whether it is in molten or solid form. Typically, the concentration of non-gaseous materials is greater than 0.02% wt. relative to the weight of the flue gas.

The method according to the invention is very suitable for incinerating solid waste material. Thus, solid fuels typically comprise more than 50%, preferably more than 75%, even more preferably more than 90% of such materials (including mixtures of domestic and industrial waste materials).

The oxygen-containing gas is typically air.

Typically, the water content of the additive material will be less than 2% wt./wt. of the additive material.

WO2013093097 and US2015/0192295 disclose the use of clay-based additives at high temperatures in incineration plants to improve properties like absorption, slagging, and/or sintering. The ash obtained once collected is less fluid than the collected ash obtained using the method according to the invention. Without wishing to be bound by any particular theory, it is believed that the better flowability of the ash collected in the present invention is due to the efficient decomposition of the specific calcium carbonate in the additive according to the present invention, which these publications do not mention.

According to an advantageous embodiment, at least 40% and more preferably at least 70% by weight with respect to the calcium carbonate is calcium carbonate in the form of: when characterized by thermogravimetric analysis at a temperature rise rate of 10 ℃ per minute in a nitrogen environment, the carbonic acid in said form has been completely decomposed when reaching a temperature of 875 ℃.

Thus, less additive is required and a reduced amount of solids must be captured before the flue gas is released into the environment, as may be desired or required.

According to an advantageous embodiment, the additive material is introduced using a plurality of injection openings, wherein the number of injection openings is selected such that the amount of flue gas per injection opening is at least 10000kg of flue gas per hour.

This embodiment has been found to work well and results in that the limited amount of pneumatic transport air applied to the incineration device is less than 1% of the amount of combustion air applied, due to the limited number of injection ports, which in turn avoids affecting the delicate balance in the incineration process (optimizing combustion, thermal efficiency, while minimizing the production of nitrogen oxides).

According to an advantageous embodiment, the solid fuel is a fuel comprising a material of non-fossil biological origin.

Non-fossil bio-derived materials are, for example, biofuels (e.g., miscanthus, wood chips).

According to an advantageous embodiment, the additive material is introduced into the flue gas containing ash, wherein the flue gas containing ash has a temperature in the range from 875 ℃ to 1050 ℃, and preferably the flue gas containing ash has a temperature in the range from 900 ℃ to 1000 ℃.

This embodiment has been found to work well. The powdered additive is broken down into smaller particles and then aggregated with non-gaseous matter from the flue gas into larger particles, effectively capturing the non-gaseous matter, resulting in ash with improved flow capability.

According to an advantageous embodiment, the amount of additive material introduced is controlled in dependence on the ash content in the flue gas comprising ash.

Ash production can be measured by weighing the amount of ash collected from the flue gas and recording the time elapsed between each collection interval. Typically, the ash collected from the incineration plant is transported for further disposal by a vehicle (e.g. a truck) which is weighed on entering (empty) and leaving (loaded with ash) the incineration plant. The weighing of the vehicle is performed by a scale, as is familiar to those skilled in the art. Amount of passing flue gas (m)³H) concentration of uncollected ash in flue gas (mg/m)³) The multiplication is performed to estimate the amount of ash not collected from the flue gas. Measurement methods for evaluating the amount of flue gas are familiar to the person skilled in the art, for example as described in the procedure NEN-EN-ISO 16931-1. Measurement methods for assessing the amount of uncaptured ash in flue gases (dust measurement) are also familiar to the person skilled in the art, for example in the specification NEN-EN-13284-1: 2001, respectively.

The term "according" indicates that the amount is directly related to the ash content in the flue gas comprising ash.

According to an advantageous embodiment, the powdered additive material is introduced at a ratio R which is 0.2 to 5 times the mass of the ash in the stream of flue gas containing ash, preferably R is a ratio between 0.3 and 2 times the mass of the ash in the stream of flue gas containing ash, and most preferably R is a ratio between 0.4 and 1.2 times the mass of the ash in the stream of flue gas containing ash.

This results in an even further improved flowability of the collected ash.

According to an advantageous embodiment, the incineration plant is part of a plant, which plant also comprises a unit for the thermal conversion of paper waste material containing kaolin, wherein kaolin is thermally treated in a fluidized bed with free air space (freeboard) in the presence of an oxygen-containing gas,

wherein the fluidized bed is operated at a temperature between 720 ℃ and 850 ℃, the temperature of the free space being 850 ℃ or less, thereby obtaining a powdered additive material, the powdered additive material being introduced into the flue gas of the incineration device containing ash

A method for preparing such a powdered additive material is disclosed in detail in WO9606057, which is incorporated by reference.

According to an advantageous embodiment, the weight/weight ratio of the switchable calcium carbonate to the clay is in the range of from 1 to 10, preferably the weight/weight ratio of the switchable calcium carbonate to the clay is in the range of from 1 to 5, and more preferably the weight/weight ratio of the switchable calcium carbonate to the clay is in the range of from 1 to 3.

Thus, the amount of additive material can be kept relatively low while improving ash capture.

According to an advantageous embodiment, the water content of the powdered material is less than 0.9% wt./wt., preferably less than 0.5% wt./wt.

This helps to rapidly disperse the powdered material into the flue gas containing ash.

Drawings

The invention will now be described with reference to the following example section and with reference to the accompanying drawings, in which,

FIG. 1 shows a schematic view of an incineration device;

FIG. 2 shows a thermogravimetric analysis (TGA) profile of various calcium carbonate-containing materials; and

figure 3 shows the fluidity of the ash obtained according to the invention (right) compared with the control section.

Detailed Description

Fig. 1 shows a plant comprising an incineration apparatus 100, which incineration apparatus 100 comprises a combustion chamber 110, a flue gas channel 120, a heat exchanger 130 and a discharge pipe 140 and a device 160 for separating ash from the flue gas, here an electrostatic filter.

A mixture of household and industry derived waste materials is fed from a fuel storage device via a hopper on the grate 170. Air is introduced into the combustion chamber 110 via the air supply duct 180.

Additive material is introduced into the flue gas channel 120 via the injection port 150.

Downstream of the heat exchanger 130, the additive material is separated from the cooled flue gas containing ash from the heat exchanger 130 using equipment 160 before the cleaned flue gas is discharged to the environment via a discharge duct 140.

The ash deposited on the heat exchanger 130 is periodically removed and discharged from the incineration apparatus via the hopper 190. Ash captured by apparatus 160 is discharged via hopper 200.

Experimental part

1. Characterization of the additive Material

The following materials were used in the incineration experiments, the properties of which are described below.

Size of powder

Laser diffraction was used to measure particle sizes in the range of 0.1 μm to 600 μm. Typically, solid state diode lasers are focused by an automatic alignment system through a measurement unit. Light is scattered by the sample particles to a multi-element detector system, which includes high-angle and backscatter detectors, to obtain a complete angular light intensity distribution. In a typical test, 10mg of sample is added to a liquid dispersion medium. The recommended dispersion medium for the samples is isopropanol. 95% by weight of the particles of samples A to F described below have a size of less than 100 μm.

Additive materials suitable for use in the present invention

-a-calcium carbonate containing material produced from deinking paper sludge prepared according to WO 0009256.

The composition of the material was determined by X-ray fluorescence. The material contains 30 mass percent of calcium carbonate; 25 mass percent of calcium oxide; 36% silica-alumina clay in the form of metakaolin.

Reference materials:

b-laboratory grade calcium carbonate (Perkin Elmer Corporation, Waltham, Massachusetts, USA (Perkin Elmer, Waltherm, Mass.) laboratory grade calcium carbonate)

-C-ground limestone (Mercury sorbents, samples from Chemical Lime Company in St. Genevieve, MO, USA (Chemical Lime of san Gienevelv, Mo.))

D-ground limestone (samples from Mercury Research Center at 19Gulf Utility, Pensacola, Florida, USA (Mercury Research Center No. 19, Pensacola, Florida))

E-ground Dolomite (sample from USA National Institute of Standards and Technology (NIST), known as Standard Reference Materials (SRM)88b)

-F-ground limestone (samples taken from the USA National Institute of Standards and Technology (NIST), referred to as Standard Reference Materials (SRM)1d SRM 1d containing argillaceous limestone)

Decomposition of materials

TGA measurements were performed using a Setam Labsys EVO TGA instrument (Setam Company, Caluire, France (Setarian, Callur, France)) at a temperature ramp rate of 10 ℃ per minute in a nitrogen atmosphere.

As can be seen from fig. 2, curves a to F correspond to the calcium carbonate-containing materials listed above, the decomposition of calcium carbonate taking place at different temperatures. For curve E, the second steep downward slope at about 950 ℃ is associated with the decomposition of calcium carbonate and the first steep downward slope at about 800 ℃ is associated with the decomposition of magnesium carbonate.

EDX measurement

The individual particles of the additive material (a) produced according to WO0009256 contain both clay and calcium compounds, which can be observed from energy dispersive X-ray spectroscopy (EDX) applied in conjunction with an Electron Microscope (EM), both methods being considered to be known to the person skilled in the art. Even EDX measurements on the smallest particles visible in EM (typically having a size of a few microns) indicate that both calcium species and silica/alumina species are present in each particle. The calcium species represent the calcium and calcium carbonate present in the additive material, while the silica/alumina species represent the clay portion present in the additive material.

2. Incineration experiment

Experiments were carried out using an incineration apparatus 100 as shown in figure 1.

The fuel processed by incinerators includes household and industry derived waste materials. Incineration results in the generation of an amount of ash in the flue gas exiting the combustion chamber 170, which is further detailed in the individual experiments 2A, 2B and 2C described below. The applied additive is produced by mixing paper residue and composting sewage sludge in a weight ratio of 85% to 15% using the method described in WO 9606057. The additive is injected into the flue gas of the incineration device leaving the incineration chamber at a height, measured from the lowest point of the grate of the incineration device, of more than 15 meters. During each of the experiments described in sections 2A, 2B and 2C below, it was observed that no flame reached this height for more than 90% of the duration of the experiment. The first heat exchanger interior-the boiler tubes-protrude into the flue gas stream 10 meters downstream of the additive injection location. The flue gas temperature at the additive injection location varies with the energy generation in the solid fuel and the incinerator, between 800 ℃ and 1050 ℃, as further detailed in individual experiments 2A, 2B and 2C. The amount of ash and the amount of additive are injected into the flue gas by pneumatic injection, typically through a steel injection port (right arrow in fig. 1) with an inner diameter of typically 32mm, which will be described in further detail in the individual experiments 2A, 2B and 2C below. The average velocity of the injected air is also further detailed in the individual experiments 2A, 2B and 2C described below.

Improved ash flow (1)

The ash is collected from a waste incineration plant operating several identical incineration furnaces and boilers. One of the furnaces has no additives applied and is taken as a reference example. The amount of ash collected from the flue gas in the reference example was about 400 kg/h. Another furnace applies the additive at a rate of 70kg/h and injects the additive through four injection ports and an injection air velocity of about 15m/s (position indicated by reference numeral 150 in fig. 1) into the flue gas at a temperature of about 950 ℃. The total amount of solids collected from the flue gas was 470 kg/h.

Within the operating limits, the further operating conditions are the same as for the material treated in the incineration plant.

The cup is filled to about half full by: 20 grams of ash (reference example; left half of fig. 3) and 20 grams of ash obtained by this process using additives (right half of fig. 3) are added, with reference number 300 and reference number 330, respectively. The cup is then tilted to observe the moment at which the ash or ash plus additive mixture reaches the pour point outside the cup. This is indicated by reference numerals 310 and 340, respectively. The material obtained using the method according to the invention flows more easily than the reference material-with a smaller inclination of the cup. The rotation required until pouring out of the cup is about 95 degrees for reference and about 80 degrees for ash plus additives. The cup is then further tilted to see when the full amount of ash (reference example) or ash plus additive is poured out of the cup, as indicated in fig. 3 by reference numerals 320 (reference ash) and 340 (ash plus additive), respectively. Also, when mixed with additives, the material flows easier-the tilt of the cup is smaller. The rotation required to completely empty the cup is about 150 degrees for reference and about 110 degrees for ash material obtained according to the present invention.

Improved ash flow (2)

Ash is collected from the flue gas of a waste incineration plant by gravity settling (fig. 1, reference numeral 190) and electro filtration (fig. 1, reference numeral 200). The two ash streams are mixed together and then loaded into a silo container (truck). Without further significant changes, two cases occur. The first case reflects normal operating procedures, with no additives applied. The second case reflects the effect of the application of the additive. The amount of normal ash collected without the application of additives was 120 kg/h. The amount of additive applied in the second case was 80 kg/h. The additive was injected into the hot flue gas through five injection ports, the flue gas temperature being about 900 ℃. The injection air velocity applied in each injection port was about 18 m/s. In both cases, the collected ash is stored in silos, from where trucks are filled for further disposal of the ash.

It was observed that in the first case (no additive applied) all three filling ports of the truck had to be used to fully load the truck. This means that the truck must be moved under the silo to position each filling port under the silo outlet chute. The total loading time exceeded 25 minutes.

It was further observed that in the second case (additive application), the truck only needs to be fully loaded using the central fill port of the truck. After the truck has positioned itself against the central filling opening, there is no longer a need to move the truck under the silo. The ash additive mixture exhibits positive flow characteristics, allowing the mixture to flow freely into the truck. The total loading time was reduced to less than 15 minutes.

2C. improved ash collection efficiency

A dose of 70 to 100kg/h of additive for a waste incineration plant was added to flue gas at a temperature of 800 to 1000 ℃ with an injection air velocity of about 15m/s through 4 injection ports (with reference numeral 150) at the locations indicated in fig. 1, resulting in a significant reduction of solids passing through the electrostatic precipitator but not removed from the flue gas stream as indicated in the table below. The following definitions apply in the following table:

ash-the amount of ash particles collected from the electrostatic precipitator filtration device in hours. The measurement is made by weighing the amount of ash produced and collected over time, by measuring the amount of ash that is transported away from the incinerator for further disposal.

Additive: an amount of additive is injected into the flue gas at a temperature of 800 to 1000 ℃ in hours through 4 injection ports (having reference numeral 150) at the positions indicated in fig. 1. The measurement is made by the discharge of a weighed dose of additive by a weighing bin (bin) over time.

Total amount: the sum of the ash shelf additives defined in the first two sentences. The measurement is made by weighing the amount of ash plus additive produced and collected over time, by measuring the amount of ash that is transported away from the incineration device for further disposal.

Increase: the amount of added or present solids (ash plus additive) in the flue gas increases mathematically before it is removed from the flue gas by the electrostatic precipitator filtration device.

Efficiency of ESP: the measured efficiency of the electrostatic precipitator filter device is defined by the mathematical division of the difference between the amount of solids present in the upstream (raw) flue gas of the ESP and the amount of solids present in the downstream (cleaned) flue gas of the ESP and the amount of solids present in the upstream (raw) flue gas of the ESP.

Discharge from ESP: the uncollected ash or ash plus the amount of additive material, which is discharged by reference numeral 140 in fig. 1, exits the electrostatic precipitator filtration device with the flue gas. From the measurement results it can be concluded that the amount of material emitted into the environment is significantly reduced (73%) when the additive according to the invention is applied.