阅读说明：本技术 飞灰的改性方法 (Modification method of fly ash ) 是由 大村昂平 关卓哉 于 2020-02-13 设计创作，主要内容包括：本发明是一种飞灰的改性方法,通过将包含未燃碳的飞灰原粉加热以降低未燃碳含量,其特征在于：(a)使用加热装置作为加热飞灰原粉的手段,其中加热通过使飞灰原粉通过加热的介质流化床来进行；(b)使高温气流通过加热装置的内部,由此形成加热的介质流化床并且进行投入介质流化床的飞灰原粉的流化输送；(c)设定高温气流的流量,使得投入加热装置中的全部量飞灰原粉通过介质流化床来加热并且从设置在加热装置的上部的取出口取出,同时形成介质流化床的介质颗粒不从取出口排出；(d)将从加热装置的取出口排出的加热的飞灰粉导入空气分级机中,以便将飞灰粉分离为细粉和粗粉；(e)将通过空气分级机回收的细粉作为改性飞灰回收；和(f)测量通过空气分级机回收的粗粉中未燃碳的含量,如果测量值大于预定阈值则将粗粉再次导入加热装置中并且再加热,并且如果测量值小于阈值则将粗粉作为改性飞灰回收。(The invention is a method for modifying fly ash, which reduces the content of unburned carbon by heating raw fly ash powder containing unburned carbon, and is characterized in that: (a) using a heating device as a means for heating the raw fly ash powder, wherein the heating is performed by passing the raw fly ash powder through a heated medium fluidized bed; (b) passing a high-temperature gas stream through the inside of the heating device, thereby forming a heated medium fluidized bed and carrying out fluidized conveyance of the fly ash raw powder charged into the medium fluidized bed; (c) setting the flow rate of the high-temperature gas flow so that the whole amount of the fly ash raw powder put into the heating device is heated by the medium fluidized bed and is taken out from a take-out port arranged at the upper part of the heating device, and simultaneously, the medium particles forming the medium fluidized bed are not discharged from the take-out port; (d) introducing the heated fly ash powder discharged from the take-out port of the heating device into an air classifier to separate the fly ash powder into fine powder and coarse powder; (e) recovering the fine powder recovered by the air classifier as modified fly ash; and (f) measuring the content of unburned carbon in the coarse powder recovered by the air classifier, re-introducing the coarse powder into the heating device and re-heating if the measured value is greater than a predetermined threshold value, and recovering the coarse powder as modified fly ash if the measured value is less than the threshold value.)

1. A method for modifying fly ash by heating raw fly ash powder containing unburned carbon and thereby reducing the content of unburned carbon, characterized in that:

a: as a means for heating the raw fly ash powder, a heating unit for heating the raw fly ash powder by passing the raw fly ash powder through a heated fluidized medium bed;

b: passing a high-temperature gas stream through the heating unit to form the heated medium fluidized bed and fluidizing and transporting the fly ash raw powder charged into the medium fluidized bed;

c: setting a flow rate of the high-temperature gas flow so that all of the fly ash raw powder charged into the heating unit is heated in the medium fluidized bed and taken out from an outlet provided at an upper portion of the heating unit, but medium particles forming the medium fluidized bed are not discharged from the outlet;

d: introducing fly ash powder after heating and discharged from the take-out port of the heating unit into an air classifier, where the fly ash powder is separated into fine powder and coarse powder;

e: recovering the fine powder recovered by the air classifier as the modified fly ash; and

f: measuring the unburned carbon content of the coarse powder recovered by the air classifier, and when the measured value is greater than a predetermined threshold value, reintroducing the coarse powder into the heating unit to be heated again, and when the measured value is less than the threshold value, recovering the powder as modified fly ash.

2. The method for modifying fly ash according to claim 1, wherein coarse powder having a measured value of unburned carbon content less than a predetermined threshold value is recovered by mixing with fine powder recovered by the air classifier.

3. The method for modifying fly ash according to claim 1, wherein the threshold value of the unburned carbon content is set to fall within a range of 0.5 to 4 mass%.

4. The method for modifying fly ash according to claim 1, wherein the classification point of the air classifier is set to fall within a range of 50 to 150 μm.

5. The process for modifying fly ash according to claim 1, wherein the raw powder of fly ash is heated in the fluidized medium bed at a temperature of 600 to 1100 ℃.

Technical Field

The present invention relates to a method for modifying fly ash by reducing the unburned carbon content of the fly ash.

Background

When fly ash is used as a material mixed in cement or as a material mixed in concrete (hereinafter, mixed material), generally, it is desirable that the content of unburned carbon in fly ash is as small as possible.

However, typically, fly ash produced from coal-fired thermal power plants contains unburned carbon in various amounts, e.g., up to about 15 mass%. Therefore, only a part of the fly ash can be used as the mixed material.

Various methods of reducing the amount of unburned carbon in fly ash have been proposed, such as a combustion method utilizing the combustibility of unburned carbon, a classification method utilizing the size of particles and their density difference, and an electrostatic separation method utilizing the charged polarity of particles.

For example, the combustion method includes a method using a rotary kiln (patent document 1), a method using cyclone (patent document 2), and a method using fluidized bed heating (patent document 3).

According to the fluidized-bed heating method, fly ash is heated by being supplied into a medium fluidized bed (hereinafter, simply referred to as a fluidized bed) formed by a heated fluidizing medium (for example, alumina having a large particle diameter), thereby reducing the content of unburned carbon therein. In this method as described in the example of patent document 3, a fluidized bed is formed by using such a fluidizing medium, so that fly ash stays in the fluidized bed for a long time, and therefore, unburned carbon is removed highly efficiently. Further, if the fluidizing medium is heated, and at the same time, if the flow rate (superficial velocity in a column) of the high-temperature gas (fluidizing gas) for fluidizing and discharging the fly ash from the fluidized bed is increased, the recovery rate of the fly ash powder being processed can be increased, however, the removal efficiency of unburned carbon is caused to decrease.

Documents of the prior art：

Patent document：

Patent document 1: japanese patent No.6038548

Patent document 2: japanese patent No.3205770

Patent document 3: japanese patent laid-open No.2000-213709

Disclosure of Invention

Problems to be solved by the invention

As can be understood from the above description, the removal efficiency of unburned carbon can be improved by the method of reducing the content of unburned carbon in fly ash based on fluidized-bed heating. In addition, the treatment efficiency of fly ash can be improved. However, it is difficult to improve both the unburned carbon removal efficiency and the fly ash treatment efficiency at the same time. That is, if the fly ash stays in the fluidized bed for a long time, the treatment efficiency of the fly ash naturally decreases. On the other hand, if the superficial velocity of the fluidizing gas is increased to improve the treatment efficiency of the fly ash, the residence time of the fly ash in the fluidized bed is shortened, resulting in a decrease in the removal efficiency of unburned carbon.

The residence time of the fly ash in the fluidized bed can also be extended by increasing the loading of the fluidizing medium forming the fluidized bed. However, there is a limit to the amount of filling of the fluidizing medium. If the filling amount is unnecessarily increased, the fluidizing medium overflows out of the fluidized bed, and a problem occurs in that the fluidizing medium is mixed in fly ash that has been already processed, or the fluidizing medium is not normally fluidized in the fluidized bed.

Accordingly, it is an object of the present invention to provide a method for modifying fly ash, which is capable of effectively reducing unburned carbon contained in fly ash.

Means for solving the problems

The present inventors have noted the fact that unburned carbon is contained in fly ash in the form of particles of various sizes, in which particles having small diameters are burned for a relatively short time and particles having relatively large diameters are burned for a relatively long time, and succeeded in effectively reducing the amount of unburned carbon contained in fly ash.

Therefore, according to the present invention, there is provided a method of modifying fly ash by heating raw fly ash powder containing unburned carbon and thereby reducing the content of unburned carbon, characterized in that:

a: as a means for heating the raw fly ash powder, a heating unit for heating the raw fly ash powder by passing the raw fly ash powder through a heated medium fluidized bed;

b: passing a high-temperature gas stream through a heating unit to form a heated medium fluidized bed and fluidizing and transporting raw fly ash charged into the medium fluidized bed;

c: setting the flow rate of the high-temperature gas flow so that all of the raw fly ash put into the heating unit is heated in the medium fluidized bed and taken out from a take-out port provided at the upper part of the heating unit, but the medium particles forming the medium fluidized bed are not discharged from the take-out port;

d: introducing the fly ash powder after heating and discharged from the take-out port of the heating unit into an air classifier, separating the fly ash powder into fine powder and coarse powder in the air classifier;

e: recovering the fine powder recovered by the air classifier as modified fly ash; and

f: the unburned carbon content of the coarse powder recovered by the air classifier is measured, and when the measured value is greater than a predetermined threshold value, the coarse powder is introduced again into the heating unit to be heated again, and when the measured value is less than the threshold value, the powder is recovered as modified fly ash.

In the present invention, it is desirable that:

(1) recovering by mixing coarse powder having a measured value of unburned carbon content less than a predetermined threshold value with fine powder recovered by an air classifier;

(2) the threshold value of the unburned carbon content is set to fall within the range of 0.5 to 4 mass%.

(3) The classification point of the air classifier was set to fall within the range of 50 to 150 μm.

(4) The raw fly ash powder is heated in a fluidized bed of media at a temperature of 600 to 1100 ℃.

ADVANTAGEOUS EFFECTS OF INVENTION

According to the present invention, it is possible to continuously recover the entire amount of raw fly ash powder subjected to the carbon content reduction treatment while sufficiently reducing the amount of unburned carbon contained in the fly ash.

Drawings

FIG. 1 is a schematic view showing a flow of a method for modifying fly ash according to the present invention.

FIG. 2 is a graph showing the relationship between the superficial velocity and the discharge rate (take-out rate) outside the heating unit of the fluidized bed.

Detailed Description

In the present invention, the raw fly ash to be subjected to the treatment for reducing the amount of unburned carbon means general fly ash generated in a coal-fired facility such as a coal-fired thermal power plant. In addition, raw fly ash includes fly ash generated from an apparatus that burns fuel other than coal and combustible waste in combination with coal. Typically, fly ash contains primarily Silica (SiO)₂) And alumina (Al)₂O₃) (these inorganic components account for 70 to 80% of the total components), and further, iron oxide (Fe)₂O₃) Calcium oxide (CaO), magnesium oxide (MgO), and the like.

The fly ash contains unburned carbon as a semi-burned carbon residue, and the content thereof is at most about 15 mass%. When fly ash is used as a mixed material, a large amount of unburned carbon (hereinafter often described as LOI) causes problems. For example, when fly ash is mixed into mortar or concrete, unburned carbon is likely to float on the surface of the mortar or concrete and form a black portion. Further, the unburned carbon may adsorb chemicals such as chemical blending agents.

The present invention reduces the amount of unburned carbon by heating by using a fluidized-bed heating unit having a fluidized bed of a medium, and efficiently recovers the obtained modified fly ash, that is, fly ash containing a reduced amount of unburned carbon.

Various methods are known for measuring the amount of unburned carbon. An example is the detection of CO produced by combustion by use of infrared light₂A method of CO gas, a method of measuring a weight loss on ignition and estimating an amount of unburned carbon from the amount of weight loss on ignition, a method of calculation based on an amount of methylene blue adsorption, a density specific gravity test method, and a method of estimating an amount of unburned carbon by irradiation with microwaves. Any of the above methods may be employed in the present invention.

Hereinafter, the amount of unburned carbon is often referred to as loi (loss on ignition).

Figure 1 illustrates the process of the invention using a fluidized bed heating unit.

In fig. 1, a fluidized-bed heating unit generally indicated by 1 has a form of an upright cylindrical shape, and forms, from the lower side upward, a combustion chamber 3, a medium fluidized bed 7 (hereinafter referred to as fluidized bed) partitioned from the combustion chamber 3 by a dispersion plate 5, and a hollow head 9.

The combustion chamber 3 is a region in which a fuel such as hydrocarbon is burned by the burner 11 to form a high-temperature gas. A theoretical amount of oxygen required for complete combustion of fuel and a gas (usually air) containing an amount of oxygen for burning unburned carbon contained in raw fly ash are supplied together with the fuel into the combustion chamber 3 and burned by the burner 11 to form a high-temperature gas. The rising flow of the high-temperature gas forms a fluidized bed 7 heated to a predetermined temperature, and further heats, fluidizes, and transports the raw fly ash powder supplied to the heating unit 1. The high temperature gas is hereinafter referred to as fluidizing gas.

In this embodiment, for example, it is desirable to supply oxygen in an amount of 1.05 to 5.0 times the theoretical amount of oxygen required for complete combustion of the fuel. If the amount is less than 1.05 times, almost all of the oxygen is consumed in the combustion of the fuel and no oxygen is left for the combustion of unburned carbon.

In the present invention, it is desirable to use air or nitrogen as the fluidizing gas from the viewpoint of cost and safety. In this case, the fluidizing gas contains nitrogen in addition to combustion gas (carbon dioxide or the like) generated by combustion of the fuel and excess oxygen (excess oxygen) that is not consumed by the combustion.

In fig. 1, white arrows indicate the flow of fluidizing gas, and black arrows indicate the flow of fly ash powder supplied into the heating unit 1.

The fluidizing gas (high-temperature gas) may also be generated by a method other than the above-described method. For example, a flowing gas is heated by a method other than the combustion method, or a system (external heating system) in which a gas is heated from the outer peripheral side of a heating power source by using an electric heater or a flame is employed.

The fluidized bed 7 is formed by heating and fluidizing medium particles 13. The raw fly ash powder is supplied through a raw material supply port 15 formed in the lower portion of the fluidized bed 7. That is, the solid medium particles held on the dispersion plate 5 are heated and floated by the fluidizing gas to thereby form the fluidized bed 7. Further, the raw fly ash is fluidized and transported due to the fluidizing gas. Here, the raw material supply port 15 is formed at the lower portion of the fluidized bed 7, so that the raw fly ash introduced through the raw material supply port 15 is sufficiently heated by the fluidizing gas and the fluidized bed 7.

In the upper part of the fluidized bed 7, an empty column 9 is formed in which no media particles 13 float. That is, the medium particles 13 forming the fluidized bed 7 are set so as not to be discharged outside the heating unit 1 by the fluidizing gas.

As the medium particles 13, it is preferable to use a material having a chemical composition similar to that of fly ash, such as SiO, for example₂、Al₂O₃、Fe₂O₃Or CaO particles or a particulate material containing these oxides as a main component, so that the characteristics of fly ash are not degraded even in the case where the medium is mixed in fly ash.

Further, it is necessary that the particle diameter of the medium particles 13 is larger than the particle diameter of the raw fly ash introduced through the raw material supply port 15. This is because if the particle size is smaller than that of the raw fly ash, the medium particles 13 are also discharged out of the unit with the flow of the fluidizing gas. I.e. it means that no empty head 7 is formed. Typically, the maximum particle size of the fly ash raw powder is about 300 μm or less, and the particle size of the media particles 13 is preferably about 0.5 to about 5 mm.

In the present invention, the raw fly ash introduced into the fluidized bed 7 is heated by being contacted with the medium particles 13 forming the fluidized bed 7 and being contacted with the fluidizing gas. Here, the heating temperature is a temperature at which unburned carbon burns, and is usually 600 ℃ to 1100 ℃, and preferably 750 ℃ to 1000 ℃. If the heating temperature is low, it becomes difficult to sufficiently remove the unburned carbon by combustion. On the other hand, if the heating temperature is not necessarily high, the fly ash may melt. Therefore, the temperature of the fluidizing gas is adjusted so that the fly ash raw powder is heated at the above temperature.

The heating temperature of the raw fly ash powder can be measured by inserting a thermocouple into the fluidized bed 7 (or into the empty head 9).

In the present invention, the raw fly ash powder is heated by the high-temperature fluidizing gas supplied as described above (and by the fluidized bed 7), and the amount of unburned carbon (LOI) in the raw fly ash powder is reduced. The heated fly ash is then discharged together with the fluidizing gas through a take-off 17 formed in the top of the tower of the heating unit 1. That is, the flow rate and flow velocity of the fluidizing gas are set so that substantially the entire amount of the raw fly ash introduced into the heating unit 1 is taken out through the take-out port 17. In practice, a balanced state is maintained by the amount of raw fly ash charged into the heating unit 1 and by the amount of fly ash heated and taken out through the take-out port 17. However, this does not exclude a case where a certain amount of fly ash may be retained in the heating unit 1 due to the structure of the heating unit 1 or the like.

The mass of the fly ash after heating and taken out through the take-out opening 17 will be smaller than the mass of the raw fly ash by at least the amount of carbon burnt out, if compared by mass.

The amount of the fluidizing gas should be appropriately set according to the form of the heating unit 1 used, and the like, in order to take out the entire amount of fly ash. However, in general, the amount of fluidizing gas supplied to the heating unit 1 (combustor 3) should be set so that the superficial velocity is 0.5 m/sec or more. Here, emptyThe tower velocity is determined by the amount (m) of fluidizing gas³In seconds) divided by the cross-sectional area (m) at the largest part of the internal diameter in the fluidized bed heating unit of the medium²) And the obtained value. The amount of fluidizing gas is calculated by using the value at the above-mentioned heating temperature.

According to the present inventors, it was found that if the superficial velocity is set to 0.5 m/sec or more, and preferably 0.6 m/sec or more, the entire amount of the fly ash raw powder can be discharged out of the heating unit 1; that is, the raw fly ash does not remain in the heating unit 1 even if continuously supplied, but can be continuously discharged (see the experimental result in fig. 2).

If the superficial velocity of the fluidizing gas becomes too great, no empty head 9 is formed and the media particles 13 are discharged together with the fly ash through the take-off 17. To avoid such inconvenience, it is generally desirable to set the superficial velocity of the fluidizing gas to a maximum of about 3 m/sec.

Here, in the present invention, the fly ash powder (heated fly ash) discharged through the take-out port 17 of the heating unit 1 is introduced into the air classifier 21 by the fluidizing gas, and classified into fine powder and coarse powder.

That is, in the above-described heating step of the raw fly ash, unburned carbon particles are burned by reaction with oxygen and disappear. However, unburned carbon particles, i.e., unburned carbon particles, are discharged through the take-out port 17 together with the ash component and the heated fly ash.

According to the studies of the present inventors, relatively large particles of unburned carbon particles may not be sufficiently burned under the aforementioned heating conditions, and may be unburned to be discharged from the heating unit 1. On the other hand, most of the small particles of unburned carbon are burned off under the above conditions.

Therefore, in the present invention, the fly ash taken out from the heating unit 1 is introduced into the air classifier 21 and separated into fine powder and coarse powder.

That is, the unburned carbon is sufficiently removed from the fine powder by combustion. Therefore, the fine powder separated by the air classifier 21 is supplied to the dust collector 23 together with the fluidizing gas, wherein the fluidizing gas is discarded and the fine powder is recovered as modified fly ash.

On the other hand, the coarse powder may be separated from the fine powder because it may contain a large amount of large-sized unburned carbon particles that are not sufficiently burned. The separated coarse powder is once fed into a temporary storage silo 25 in which the amount of unburned carbon (LOI) is measured by an LOI measuring device 27 provided in the silo 25. When the LOI is below a preset threshold value (LOI is less than or equal to the threshold value), the coarse powder is recovered to be used as modified fly ash. When the LOI exceeds the preset value (LOI > threshold), the meal is returned to the heating unit 1 (fluidized bed 7) where it is reheated to reduce the LOI. Here, in the case where the LOI is equal to the threshold value (LOI ═ threshold value), it is natural that the coarse powder may be returned to the heating unit 1 to be subjected to the reheating process.

The threshold value should be appropriately set according to the LOI required for fly ash used as a mixed material of cement and concrete. For example, the threshold value is preferably set in the range of 0.5 to 4 mass%, and particularly in the range of 0.5 to 3 mass%.

The coarse meal recovered as modified fly ash from the temporary storage silo 25 has a low LOI. Therefore, the coarse powder can be naturally recovered by mixing with the modified fly ash (fine powder) recovered from the dust collector 23.

Currently, studies are continued to remove unburned carbon having a large particle size by means of air classification by utilizing the principle that the unburned carbon contained in the unburned carbon-containing fly ash has a large particle size. However, the unburned carbon particles have a small specific gravity and are therefore contained in a large amount in the fine powder. Therefore, in practice, the fly ash cannot be substantially separated into coarse particles and fine particles containing unburned carbon in different amounts by means of air classification. On the other hand, according to the present invention, fly ash is heated at one time and then separated by air. Therefore, the unburned carbon having a large particle diameter is distributed toward the coarse particle side and is reintroduced into the heating unit 1 in accordance with the LOI of the coarse particles, so that the unburned carbon content can be effectively reduced.

In the present invention described above, it is desirable to set the classification point in the air classifier in the range of 50 to 150 μm and particularly 100 to 150 μm. The proportion of unburned carbon recovered as the coarse powder increases as the classification point becomes smaller. However, as the classification point becomes smaller, it becomes more likely that even those particles that are not required to be recovered as coarse powder will be recovered. Therefore, from the viewpoint of efficient operation, it is desirable to set the classification point within the above range.

The air classifier 21 is not particularly limited, and for example, an air classifier using a centrifugal force field, a classifier using a gravitational field, or a classifier using an inertial force field can be used.

The dust collector 23 for collecting the fine powder classified by the air classifier 21 is also not particularly limited, and any type of dust collector, such as an electric dust collector, a gravity type dust collector, or a centrifugal type dust collector, may be used.

Furthermore, as already described, the LOI measuring device 27 provided for the temporary storage silo 25 will perform LOI measurements according to any known method.

Examples

The present invention will now be described by the following experimental examples.

< experiment >

Fly ash raw powder having an LOI of 10.0 mass% was prepared. The average particle size was 44 μm, while the maximum particle size was about 300. mu.m.

The fly ash raw powder was supplied to the heating unit 1 shown in fig. 1, and fluidizing gas (air) was supplied at a superficial velocity of 0.64 m/sec, and the heating temperature was 850 ℃. The raw fly ash is thus heat-treated and separated into coarse and fine powders. The classification point was set to about 50 μm. The fine powder and the coarse powder were recovered at a ratio of 63 mass% and 37 mass% respectively with respect to the raw fly ash powder, and the sum of the fine powder and the coarse powder was 100 mass%.

The LOI in the fine powder was 1.1 mass%, while the LOI in the coarse powder was 5.0 mass%. LOI in the fines was sufficiently low. Therefore, the fine powder can be easily used as modified fly ash. On the other hand, LOI in the meal was high. Accordingly, meal needs to be reheated when it is used in many applications.

LOI is measured according to the loss on ignition test method prescribed in JIS A6201.

Further, by changing the superficial velocity of the fluidizing gas, the fly ash raw powder was heat-treated to measure the superficial velocity and the discharge rate of the fly ash discharged from the heating unit 1 (the ratio of the fly ash to the supplied fly ash raw powder). The results are shown in FIG. 2.

As can be understood from the results of fig. 2, if the superficial velocity is set to 0.5 m/sec or more, and particularly 0.6 m/sec or more, almost all of the fly ash raw powder can be discharged out of the unit without staying in the unit.

Description of the reference numerals：

1: heating unit

3: combustion chamber

5: dispersion plate

7: fluidized bed

9: hollow head

11: burner with a burner head

13: medium particle

15: raw material supply port

17: taking-out port

21: air classifier

23: dust collector

25: temporary storage silo

27: LOI measuring device