JPH11169631A - Dedusting device of dusty high-temperature high-pressure gas and dedusting method therefor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a highly durable dedusting device which is capable of preventing the concentration of the fine ash dust to a precision dedusting device and is capable of stably executing the dedusting from a dusty high-temp. high- pressure gas. SOLUTION: This dedusting device for the dusty high-temp. high-pressure gas has a coarse dedusting device 3 which coarsely dedusts the dusty high-temp. high-pressure gas generated in a dusty high-temp. high-pressure gas generator 1 and the precision dedusting device 5 which precisely dedusts the gas subjected to the coarse dedusting. The dedusting device has a grain size distribution regulating pipe 9 for regulating the grain size distribution of the ash dust in the gas flowing into the precision dedusting device 5 between a combustion gas flow passage 2 and a coarse dedusted gas flow passage 41.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a deduster for a high temperature and high pressure gas containing dust generated in a blast furnace, a kiln or the like, which mainly uses solid fuel such as coal power generation, refuse power generation, or municipal waste incinerator. And a dust removal method.

[0002]

2. Description of the Related Art In recent years, a pressurized fluidized bed boiler mainly using solid fuel such as coal, a combustion device operated under pressure such as a direct coal combustion device, a combustion device such as a municipal solid waste incinerator, a blast furnace and a kiln. As for the combustion gas discharged from such devices, dust removal using a dust removal device provided with a ceramic filter, a louver dust removal device, a cyclone, a multi-cyclone, or a dust removal device combining these is generally performed. Among them, the pressurized fluidized bed combined cycle system is a system that combines steam turbine power generation driven by steam generated from a fluidized bed boiler installed in a pressure vessel and gas turbine power generation using boiler exhaust gas. And high denitrification and desulfurization performance, which has attracted particular attention. In this pressurized fluidized bed combined cycle system, a steam turbine shares about 80% of the power generation output, and a gas turbine shares the remaining about 20%. Hereinafter, a conventional pressurized fluidized-bed combined power generation system and a dust removing device for dust-containing high-temperature and high-pressure gas generated from a pressurized fluidized-bed boiler will be described with reference to the drawings.
FIG. 11 is a schematic diagram of a main part of a conventional combined pressurized fluidized bed power generation system, and FIG. 12 is a cross-sectional view of a main part of a precision dust removing device using a plurality of ceramic tube filters. 11, reference numeral 1 denotes a pressurized fluidized-bed boiler of a high-temperature and high-pressure dust-containing gas generator, 1a denotes a heat transfer tube buried in a fluidized bed of the pressurized fluidized-bed boiler 1, and 2 denotes a top of the pressurized fluidized-bed boiler 1. The provided combustion gas flow path, 3 is a coarse dust removal device provided at the outlet of the combustion gas flow path 2, 4 is a coarse dust removal gas flow path coarsely removed by the coarse dust removal device 3, and 5 is A precision dust removing device constituted by a ceramic tube filter, 6 is a clean gas passage precisely removed by the precision dust removing device, 7 is a gas turbine, and 8 is a generator. FIG.
In 2, 11 is a pressure vessel of the precision dust removing device 5, 12 is a ceramic tube filter, 13 is a top chamber, 14 a, 14 b, 14 c, and 14 d are support plates, 15
a, 15b, 15c are dust chambers, 16 is a hopper, 17a,
17b and 17c are ejectors, 18a, 18b and 18c are backwash nozzles, 19a, 19b and 19c are high-speed backwash valves, 2
Reference numerals 0a, 20b, and 20c denote backwash air inflow paths. The operation of the conventional pressurized fluidized bed combined cycle system configured as described above will be described below. In the pressurized fluidized-bed boiler 1 of the dust-containing high-temperature and high-pressure gas generator, a mixture of coal and limestone is cooled by air from a compressor (not shown).
Fluidized under pressure of 6 to 1.6 MPa and 800 to 9
Burns at about 50 ° C. The heat generated by the combustion is recovered as steam by the heat transfer tube 1a in the fluidized bed, and drives a steam turbine generator (not shown) to generate power. On the other hand, the combustion gas containing a large amount of ash dust generated from the dust-containing high-temperature and high-pressure gas generator 1 rises from the upper surface of the fluidized bed at a predetermined speed of 1.0 ± 0.5 m / s, The flow rate becomes several m / s, and most of the ash dust in the dust-containing gas sent to the coarse dust removal device 3 is removed. The coarsely-dusted gas passes through the coarse-dust gas flow path 4 and is precision-dusted by the precision dust-removing device 5. The finely-dusted gas is supplied from the clean gas passage 6 to the gas turbine 7.
To drive the generator 8 to generate power. Here, a cyclone or the like having excellent ability to remove a large amount of ash is used as the coarse dust removing device 3, and a precision dust removing device 5 for removing fine ash dust from the coarse dust gas discharged from the coarse dust removing device. In addition to ceramic tube filters, ceramic candle filters, ceramic honeycomb filters, metal filters, and the like are used. In the pressurized fluidized bed combined cycle system, the fuel and air are increased in order to increase the output, so that the furnace pressure is almost proportional to the gas turbine output. If the pressure loss of the dust removing device is large, increasing the output will exceed the design differential pressure of the gas turbine, so the pressure loss of the dust removing device is required to be as small as possible.

As shown in FIG. 12, a precision dust removing device 5 includes a plurality of ceramic tube filters 12 in a pressure vessel 11.
The interior of the pressure vessel 11 is divided into three dust removal chambers 15a, 15b, 15c, a top chamber 13, and a hopper 16 by support plates 14a, 14b, 14c, 14d. Ejectors 17a, 17b, 17c are connected to the dust removal chamber and the clean gas discharge pipe 6
In one. The ejectors 17a, 17b,
Backwash nozzles 18a, 18b, 18c are connected to the base of 17c. The coarse dust gas coarsely dusted by the coarse dust removal device 3 flows into the pressure vessel 11 from the coarse dust gas flow path 4 at a flow rate of several tens m / s, and flows into the ceramic tube filter 12 from the top chamber 13. Inflow. Since the ceramic tube filter 12 has a porous structure, the gas is filtered and flows out from the inner surface of the tube filter to the outer surface of the tube filter while flowing down. The gas thus purified passes through the clean gas flow path 6 via the ejectors 17a, 17b, 17c, is sent to the gas turbine 7, and is supplied to the generator 8
To generate electricity. Since the ash dust collected from the gas adheres to the inner surface of the ceramic tube filter 12, the pressure difference between the inside and the outside of the ceramic tube filter increases with time. Therefore, the high-pressure air flow path 2
0a, 20b, 20c, high-speed backwash valve 19a,
19b and 19c are sequentially opened, and the backwash nozzles 18a and 18c are opened.
Supersonic high-pressure air is sent from b and 18c into the pressure vessel 11 and blown from the outer surface side of the ceramic tube filter 12 to peel off and remove ash dust attached to the inner surface. The separated ash falls in the ceramic tube filter 12 and is sent from the hopper 16 to an ash dust treatment device (not shown).

[0004]

However, the above-mentioned conventional dust removing apparatus and dust removing method have the following problems. (1) Alkaline components (Na, K) in solid fuels such as coal
Etc.) are released as chlorides in the course of combustion and form alkali sulfates by a reaction as shown in Chemical Formulas 1 and 2 with sulfur oxides in the combustion gas. This alkali sulphate is a low melting point compound that melts on the ash dust particles to produce extremely adherent ash.

Embedded image

Embedded image It has been confirmed that the alkali concentration in the combustion gas depends on the alkali content in the solid fuel, but is also affected by the combustion temperature and the halogen content in the solid fuel. Also,
The ash dust flowing into the precision dust removing device 5 is a fine particle having an average of 3 μm, which tends to adhere and consolidate due to an increase in the specific surface area, and firmly adheres to the inner surface of the ceramic tube filter by the pressure of the gas flow during normal filtration. It has been known. In addition, calcium carbonate such as limestone mixed for desulfurization decarboxylates in the combustion device by the reaction shown in (Chem. 3), but reacts with carbon dioxide gas in the combustion gas as shown in (Chem. 4). It is known to produce calcium carbonate with high adhesion.

Embedded image

Embedded image For these reasons, ash dust adheres firmly to the inner surface of a precision dust removal device such as a ceramic tube filter, lowering the dust removal efficiency, and also causing damage to the dust removal device due to blockage,
A great deal of labor is required for the maintenance, and there is a problem that pressure loss occurs due to the attached ash dust, thereby lowering the operation efficiency of the equipment. (2) As a countermeasure, a cyclone or the like is used as a coarse dust removing device on the upstream side, but the ability to collect fine ash dust having a particle size of about several μm is inferior. However, there is a problem that the dust is concentrated on the precision dust removing device and easily adheres firmly to the inner surface of the ceramic tube filter as described above. (3) If ash dust adheres to the inner surface of the ceramic tube filter and the pressure loss increases, the output of the gas turbine is reduced, so that the power generation output is limited or the power generation efficiency is reduced. (4) The pressure, time and frequency of backwashing must be increased in order to remove the attached ash dust, and the amount of nitrogen purge from the hopper and the like accompanying backwashing air and backwashing increases, thereby increasing utility. There was a problem. (5) Due to the adhesion of ash dust, the temperature difference between the inside and outside of the ceramic tube filter and the temperature difference in the axial direction are widened, and thermal stress is generated. There has been a problem that the strength of the ceramic tube filter is reduced due to the thermal stress and a combined stress such as a stress due to repeated backwashing and the ceramic tube filter is easily broken. (6) There is a problem that the life of the ejector, the backwash nozzle and the like, which are accessories of the precision dust removing device, is shortened by the impact due to the repetition of the backwash. (7) In order to prevent the breakage of the ceramic tube filter, it is necessary to increase the area of the filter or to increase the filter to reduce the filtration flow rate, so that the equipment becomes large-scale and the heat loss increases. There is a problem that the gas temperature decreases and the gas turbine output decreases.

(8) To solve these problems, Japanese Unexamined Patent Publication No. 7-96127 discloses a fly ash method in which fine ash dust in a dust-containing gas is aggregated and granulated by a stainless steel net to make it coarse. There is disclosed a dust remover including a granulator and a precision dust remover made of ceramic, and a method of removing dust-containing gas using the dust remover. However, it has been found that the dust removing device and the dust removing method disclosed in the above publication have the following problems. a. The large size fly ash granulator makes the equipment larger and increases the calorific value and pressure loss, lowering the energy efficiency when used for power generation, etc., and integrating it into existing equipment on a large scale. However, there is a problem that the installation work is inferior due to the necessity of complicated construction. b. Since a stainless steel net is used, there is a problem that when dust-containing combustion gas flows in a pressurized fluidized bed combined power generation system at 800 ° C. or higher, deterioration is large and durability is poor.

SUMMARY OF THE INVENTION The present invention solves the above-mentioned conventional problems, and prevents the fine ash dust from concentrating on a precision dust removing device, and has a durability capable of stably removing dust from a dust-containing high-temperature and high-pressure gas. Provide high-quality dust removal equipment, and prevent clogging and blockage of precision dust removal equipment such as ceramic tube filters, reduce pressure loss, increase energy efficiency such as power generation, and provide precision dust removal equipment such as ceramic tube filters. It is an object of the present invention to provide a method for removing dust from high temperature and high pressure gas containing dust, which can prevent breakage of the gas and enable stable operation for a long period of time.

[0007]

SUMMARY OF THE INVENTION In order to solve the above-mentioned conventional problems, a dust-containing high-temperature and high-pressure gas dedusting apparatus according to the present invention is provided with a coarse dust-removing apparatus. A dust removing device for dust-containing high-temperature and high-pressure gas, comprising: a coarse dust removing device that performs dust removal; and a precision dust removing device that precisely removes the coarsely dusted gas. And a particle size distribution adjusting pipe for adjusting the particle size distribution of the ash dust is provided between the combustion gas flow path and the coarse dust gas flow path. With this configuration, a large-sized granulation device or the like is not required, and the device can be downsized. Therefore, loss of heat and pressure can be minimized, and energy efficiency used for power generation and the like can be increased. In addition, a small-scale improvement of existing equipment can provide a dust removing device having the above-described excellent effects. Further, the method for removing dust from the dust-containing high-temperature and high-pressure gas of the present invention includes a coarse dust-removing step in which the dust-containing high-temperature and high-pressure gas generated from the dust-containing high-temperature and high-pressure gas generator passes through a coarse dust remover to roughly remove the dust. A precision dust removal step of precision dust removal by passing the removed gas through a precision dust removal device, wherein the dust containing high temperature and high pressure gas generated from the dust containing high temperature and high pressure gas generator is provided. A configuration is provided in which a part of the dust-containing high-temperature and high-pressure gas is caused to flow through the particle size distribution adjusting tube and flow into the precision dust removing device. With this configuration, the width of the particle size distribution of the ash dust flowing into the precision dust removal device is widened, and the amount of coarse ash dust particles is increased. Therefore, it is possible to prevent ash dust from adhering to the precision dust removal device such as a ceramic tube filter. Can,
Since the pressure loss can be further reduced, the efficiency of power generation and the like can be increased. In addition, the thermal stress on the dust removal part of the precision dust removal device such as a ceramic tube filter can be reduced, and the frequency, time, pressure, etc. of backwashing can be reduced. And reliability can be improved. Further, since the frequency, time, and pressure of backwashing can be reduced, the internal rate can be reduced, and the power transmission end efficiency can be improved.

[0008]

DETAILED DESCRIPTION OF THE INVENTION The dust-removing device for dust-containing high-temperature and high-pressure gas according to the first aspect of the present invention roughly removes dust-containing high-temperature and high-pressure gas generated by a dust-containing high-temperature and high-pressure gas generator. Equipment and
A precision dust removal device for precision dust removal of coarsely-dusted gas, comprising: a dust removal device for dust-containing high-temperature and high-pressure gas, comprising: a particle size distribution of ash dust in the gas flowing into the precision dust removal device. A configuration is provided in which a particle size distribution adjusting tube to be adjusted is provided between the combustion gas flow path and the coarse dust gas flow path. With this configuration, the width of the particle size distribution of the ash dust flowing into the precision dust removing device is widened, and the amount of coarse ash dust particles increases, so that the attachment of the ash dust to the ceramic tube filter decreases and the pressure loss can be reduced. Therefore, there is an effect that the efficiency of power generation and the like can be increased. In addition, since the thermal stress on the ceramic tube filter can be reduced and the frequency of backwashing can be reduced, there is an effect that the durability and reliability of the ceramic tube filter can be improved. Since the frequency of backwashing can be reduced, the in-house rate can also be reduced, which has the effect of improving the efficiency of power generation and the like. It is possible to stably operate the precision dust removing device by small-scale improvement of existing equipment, and to obtain a dust removing device excellent in durability. In addition, one or more orifices are further provided in the particle size distribution adjusting pipe, and the gas flow rate for particle size distribution adjustment and the particle size distribution of ash dust in the gas are controlled by setting the orifice diameter and the number of orifices to be provided. can do. When the orifice is not provided, the flow rate of the gas for adjusting the particle size distribution and the width of the adjustment of the particle size distribution can be increased by setting the flow rate of the gas for adjusting the particle size distribution to be large.
Further, by changing the position of the particle size distribution adjusting gas outlet, the particle size distribution in the particle size distribution adjusting gas can be set optimally, so that the set position is appropriately determined according to the type and size of the combustion device. Must be set.

According to a second aspect of the present invention, there is provided a dust removing device for dust-containing high-temperature and high-pressure gas, comprising: a coarse dust removing device for roughly removing dust-containing high-temperature and high-pressure gas generated by a dust-containing high-temperature and high-pressure gas generator; A dust removal device for dust-containing high-temperature and high-pressure gas, comprising: a precision dust removal device for precision dust removal of the removed gas, wherein a particle size distribution of ash dust in the gas flowing into the precision dust removal device is adjusted. A particle size distribution adjusting pipe is provided between the top of the dust-containing high-temperature and high-pressure gas generator and the coarsely-dusted gas flow path. With this configuration,
In addition to the function of claim 1, by providing a particle size distribution adjusting tube between the top of the dust-containing high-temperature and high-pressure gas generator and the coarsely-dusted gas passage, the particle size distribution adjusting tube can be shortened. In addition to reducing the size of the entire device, reducing the flow velocity and heat loss of the particle size distribution adjusting gas flowing through the particle size distribution adjusting tube, it is possible to improve power generation efficiency and efficiently remove dust accurately. The particle size distribution of the ash dust flowing into the apparatus can be adjusted.

According to a third aspect of the present invention, there is provided a dust-removing device for dust-containing high-temperature and high-pressure gas, comprising: a coarse dust-removing device for roughly removing dust-containing high-temperature and high-pressure gas generated by a dust-containing high-temperature and high-pressure gas generator; A precision dust removal device for precision dust removal of the dust-removed gas, comprising: a dust-containing high-temperature and high-pressure gas removal device, comprising: a ash dust removed by the coarse dust removal device; A dust circulating section circulating in the generator, and a particle size distribution of ash in the gas flowing into the precision dust removing device which is connected between the top of the high-temperature and high-pressure gas generating device and the coarse dust removing gas flow path. And a particle size distribution adjusting tube. With this configuration, even in a dust-containing high-temperature and high-pressure gas generator such as a circulating fluidized bed having a superficial velocity of 5 to 7 m / s, the particle size distribution of ash dust flowing into the precision dust remover can be adjusted. This has the effect of reducing the burden on the dust removal device and achieving stable operation. In addition, since the ash dust containing unreacted calcium oxide that has not been consumed in the dust-containing high-temperature and high-pressure gas generator can be effectively used, such as circulating, the desulfurization effect in the dust-containing high-temperature and high-pressure gas generator is improved. It has the effect of being able to.

According to a fourth aspect of the present invention, there is provided a dust-removing apparatus for dust-containing high-temperature and high-pressure gas according to any one of the first to third aspects. Clogging degree detection means in the dust removal device, and particle size distribution control means for controlling the particle size distribution of ash dust particles in the gas based on the degree of clogging detected by the clogging degree detection means It has a configuration. With this configuration, it is possible to control the particle size distribution based on the degree of clogging detected by the degree of clogging of the precision dust removal device, so that the load on the precision dust removal device can be reduced and set optimally. And has the effect that long-term stable operation can be achieved. In addition, when clogging occurs due to a rapid change in the combustion state, the clogging can be eliminated by adjusting the particle size distribution. Here, the clogging degree detecting means is preferable because it is easy to measure a change in the pressure loss amount in the precision dust removing device with a pressure gauge or the like. Further, as the particle size distribution adjusting means, a gas injection device for air or the like, a gas inflow control damper, and a particle size distribution adjusting tube, which are provided in a particle size distribution adjusting gas take-out portion of the particle size distribution adjusting tube, are provided. Examples include a gas injection device and a control valve. In particular, when the particle size distribution is adjusted with a gas injection device such as air, the ash dust with a large particle size and large inertia can be mainly selectively introduced into the precision dust removal device by gas injection. The effect of preventing the dust removing device from being clogged can be increased.

According to a fifth aspect of the present invention, there is provided a dust removing method for dust-containing high-temperature and high-pressure gas, wherein the dust-containing high-temperature and high-pressure gas generated from the dust-containing high-temperature and high-pressure gas generator is passed through a coarse dust removing device. A dust-removing high-temperature and high-pressure gas removing method, comprising: a dust-removing step; and a precision dust-removing step of precision-removing the coarsely-removed gas through a precision-removing device. A configuration is provided in which part of the dust-containing high-temperature and high-pressure gas generated from the generator passes through the particle size distribution adjusting tube and flows into the precision dust removing device. With this configuration, the width of the particle size distribution of the ash dust flowing into the precision dust removal device is widened, and the amount of coarse ash dust particles increases,
This has the effect of preventing ash dust from adhering to the ceramic tube filter in a compact manner, reducing the pressure loss and increasing the efficiency of power generation and the like. In addition to reducing the thermal stress on the precision dust removal device such as a ceramic tube filter, the backwashing time, backwash frequency and backwash pressure can be reduced, so that the durability and reliability of the ceramic tube filter etc. can be reduced. Can be improved. Further, since the backwashing time, the backwashing frequency, and the backwashing pressure can be reduced, the in-house ratio and utility can be reduced, and the efficiency of power generation and the like can be improved. Further, the ceramic tube filter is less likely to be clogged by ash dust even during long-term operation, and the amount of generated stress is reduced, so that an accident such as breakage can be prevented.

According to a sixth aspect of the present invention, there is provided a dust removing method for a dust-containing high-temperature and high-pressure gas according to the fifth aspect, wherein the dust-containing high-temperature and high-pressure gas is removed through the particle size distribution adjusting tube. The high-temperature high-pressure gas amount is 1 to 95%, preferably 3 to 85%, more preferably 8 to 50% of the total dust-containing high-temperature high-pressure gas amount. This configuration has an effect that the particle size distribution of the ash dust flowing into the precision dust removing apparatus can be adjusted to adapt to the particle size distribution of the ash dust that varies depending on the type of coal and changes in the combustion state. In addition, there is an effect that the amount of gas and the amount of ash passing through the particle size distribution adjusting pipe can be controlled in the above range according to a rapid change in the combustion state. Here, as the amount of the dust-containing high-temperature and high-pressure gas passing through the particle size distribution adjusting pipe becomes smaller than 8%, it tends to easily occur that it is difficult to increase the particle size distribution depending on the type of the solid fuel,
Since the load on the precision dust removing device tends to be difficult to reduce, and as the amount exceeds 50%, the amount of ash dust increases, so that the degree of wear inside each gas passage increases and the coarse dust removing device increases. Since the amount of gas flowing into the device is reduced, the efficiency of the coarse dust removing device tends to decrease, and neither is preferable. The tendency is further increased as the amount of the dust-containing high-temperature and high-pressure gas is less than 3% or more than 85%, and this tendency is significantly increased as the amount is less than 1% or more than 95%. . Hereinafter, specific examples of the embodiments of the present invention will be described with reference to the drawings.

(Embodiment 1) FIG. 1 is a schematic diagram of a main part of a dust-containing high-temperature and high-pressure gas dedusting apparatus according to Embodiment 1 of the present invention. In FIG. 1, 1 is a pressurized fluidized-bed boiler of a dust-containing high-temperature and high-pressure gas generator, 1a is a heat transfer tube disposed in a fluidized bed, 2 is a combustion gas channel, 3 is a coarse dust removing device, and 4 is a coarse dust removing device. A dust removal gas passage, 5 is a precision dust removal device, 6 is a clean gas passage, 7 is a gas turbine, and 8 is a generator, all of which are the same as those in the conventional example. The description is omitted here. Reference numeral 9 denotes a coarse dust removal device 3 which is provided in parallel with the combustion gas flow path 2 to remove the combustion gas generated from the dust-containing high-temperature and high-pressure gas generator 1.
This is a particle size distribution adjusting tube that flows into the precision dust removing device 5 without passing through the pipe. The point that the dust removing apparatus in the present embodiment differs from the conventional example is that a particle size distribution adjusting pipe 9 is provided between the combustion gas flow path 2 and the coarse dust removing gas flow path. As a result, a predetermined amount of the large-size ash dust in the combustion gas flows into the precision dust removal device 5 without being coarsely removed, so that the particle size distribution of the ash dust flowing into the precision dust removal device 5 can be adjusted. In addition, since the amount of coarse ash particles increases, the specific surface area is reduced, and the ash dust has the effect of preventing the fine ash dust from being compacted and firmly attached to the inner surface of the ceramic tube filter. As a result, there is an effect that clogging and blockage in the ceramic tube filter can be reduced. Further, since fine ash dust is prevented from adhering to the inner surface of the ceramic tube filter in a compact manner, ash dust can be easily peeled off and removed by backwashing, and the frequency of backwashing can be reduced.

(Embodiment 2) FIGS. 2A and 2B
FIG. 4 is a schematic diagram of a main part of a particle size distribution adjusting tube according to Embodiment 2 of the present invention. 2 (a) and 2 (b), 2a
Is a combustion gas passage, 3 is a coarse dust remover, 4a is a coarse dust remover 3
The coarse dust gas that has been coarsely dusted by the precision dust removal device (not shown)
The coarse dust gas flow path flowing into the boiler top manifold 21 is disposed in the boiler top manifold 21 and communicated with the coarse dust gas flow path 4a, and 22 is one end of a pipe inside the boiler top manifold 21. Is a particle size distribution adjusting gas take-out portion of the particle size distribution adjusting tube 9a formed by splitting into half, and 23 is an orifice for adjusting a flow rate provided in the particle size distribution adjusting tube 9a. The orifice 23 may not be provided depending on the size of the inner diameter of the particle size distribution adjusting tube 9a. The upper and lower elbows of the particle size distribution adjusting tube 9a may be T-shaped to prevent abrasion due to ash dust, depending on the type of solid fuel. In FIG. 2 (b), reference numeral 9a 'denotes a straight tubular particle size distribution adjusting tube which is disposed on the upper surface of the boiler top manifold 21 and is connected to the coarse dust removal gas passage 4a. Thus, the particle size distribution adjusting pipe 9a can be disposed above the boiler (not shown), so that the entire apparatus can be made compact. Also, one or more orifices 23 are arranged in the particle size distribution adjusting pipe 9a, and the diameter of the orifices and the number of the orifices are appropriately set to control the gas flow rate for adjusting the particle size distribution. The particle size distribution of the ash dust can be adjusted, and the particle size of the ash dust in the gas flowing into the precision dust removing device can be set to an optimum value. Here, as the material of the orifice, ceramics having excellent heat resistance and abrasion resistance, Avesta cast steel, and the like are used.
The orifice diameter depends on the diameter of the particle size distribution adjusting tube, but it is preferably 0.1 to 0.9 times the particle size distribution adjusting tube, and more preferably 0.2 to 0.9 times.
Eight times is desirable. This is to give the maximum effect without sacrificing the flow rate. Here, if the gas flow rate for particle size distribution adjustment in the case where the orifice is not provided is set to a large value in advance, the range of particle size distribution adjustment by the orifice can be widened, so that the country or grade of coal production, desulfurization agent Optimum values can be set in advance for the amount of ash dust and particle size distribution that greatly vary depending on the type and input amount of ash and combustion conditions. Further, as shown in FIG. 2B, a straight tubular particle size distribution adjusting pipe 9a 'may be provided on the upper surface of the boiler top manifold 21, and may be connected to the coarse dust gas flow path 4a. This is because the particle size distribution adjusting tube does not have a curved portion and the flow path can be shortened, and the loss of gas flow rate and heat can be suppressed.

(Embodiment 3) FIG. 3 is a schematic diagram of a main part of a particle size distribution adjusting tube according to Embodiment 3 of the present invention. FIG.
2a is a combustion gas flow path, 3 is a coarse dust removing device, 4a
Is a coarse dust gas passage, 21 is a boiler top manifold, 2
Reference numeral 3 denotes an orifice, which is the same as that of the second embodiment, and therefore, is denoted by the same reference numeral and description thereof is omitted. Reference numeral 9b denotes a coarse dust removal gas passage 4 which is disposed on the boiler top manifold 21.
a, a particle size distribution adjusting gas outlet 31 formed by half-breaking one end of the particle size distribution adjusting tube 9b fitted into the boiler top manifold 21; A gas injection device 32a provided on the upper portion of the diameter distribution adjusting gas extraction portion 31 and injecting a gas such as air;
Is a gas injection hole formed by drilling one or more gas injection holes in the upper pipe of the gas outlet, 33 is a gas injection amount control valve provided in the gas injection device 32, and 34 is a precision dust removal device (not shown). The control valve 33 detects the degree of clogging (differential pressure, etc.).
Is a particle size distribution control means for controlling the degree of opening and closing. Accordingly, the control valve 33 is controlled by the particle size distribution control means 34 in response to the amount of ash dust in the combustion gas, the state of the particle size distribution, and the change in the degree of clogging of a precision dust removing device (not shown). This has the effect that the gas flow rate for adjusting the particle size distribution can be optimally controlled by a simple operation of adjusting the opening / closing degree of the gas. In addition, since the flow of gas such as air or nitrogen to the opening and closing of the valve has a quick response, there is an effect that the particle size distribution can be quickly controlled to an optimum value. By applying a back pressure from the gas injection device 32, it is possible to prevent ash dust particles having a small particle size and a small inertia force from flowing into the particle size distribution adjusting tube 9b, so that ash dust particles having a large particle size and a large inertia force are selected. In this case, the particle size distribution of the precision dust removing device is expanded by flowing the particles into the particle size distribution adjusting pipe 9b, thereby improving the effect of preventing clogging and clogging. Here, as the gas to be injected from the gas injection device, compressed air in a pressure vessel (not shown) in which a pressurized fluidized-bed boiler is installed can be used as it is, or a compressed air can be separately used by using a compressor or the like. And nitrogen or the like can be introduced. Further, when the valve of the gas injection device is disposed outside the pressure vessel (not shown), the gas injection amount can be easily controlled, and a valve material having relatively low heat resistance can be used. preferable.

(Embodiment 4) FIG. 4 is a schematic view of a main part of a particle size distribution adjusting tube according to Embodiment 4 of the present invention. FIG.
2a is a combustion gas flow path, 3 is a coarse dust removing device, 4a
Is a coarse dust gas passage, 21 is a boiler top manifold, 2
Numeral 2 denotes a particle size distribution adjusting gas take-out unit, which is the same as that of the second embodiment. 9c is a particle size distribution adjusting tube, 41a and 41b are gas injection devices such as air and nitrogen arranged in upper and lower elbows of the particle size distribution adjusting tube 9c, and 42a and 42b are gas injection devices 4
These are the control valves 1a and 41b. This makes it possible to quickly respond to changes in the state of the combustion gas and the state of the precision dust removal device (not shown), and to optimally control the gas flow rate for adjusting the particle size distribution. In particular, when the amount of ash dust increases rapidly and the gas flow rate to the particle size distribution adjusting pipe 9c becomes excessive, the control valves 42a and 42b are opened to inject a gas such as air or nitrogen to adjust the particle size distribution. By controlling the flow rate of the gas for adjusting the particle size distribution flowing into the pipe 9c, large-size ash dust having a large inertia force can be selectively introduced into the precision dust removing device, and the amount and size distribution of the ash dust can be reduced. Can be controlled.
Here, the above-mentioned gas can be used as the gas to be injected from the gas injection device. Note that coarse ash dust having a particle size distribution collected from the coarse dust removing device 3 may be accompanied by the gas injected from the gas injection device. This is because the width of the particle size distribution adjustment can be increased, and unreacted calcium oxide and the like can be effectively used.

(Embodiment 5) FIG. 5 is a schematic diagram of a main part of a particle size distribution adjusting tube according to Embodiment 5 of the present invention. FIG.
2a is a combustion gas flow path, 3 is a coarse dust removing device, 4a
Is a coarse dust removal gas passage, 9a is a particle size distribution adjusting tube, 21 is a boiler top manifold, and 23 is an orifice, which are the same as those of the other embodiments of the present invention. The description is omitted. Reference numeral 51 denotes a rotatable gas inflow which is provided below the inlet 22 for the particle size distribution adjusting gas flowing into the particle size distribution adjusting pipe 9a and which can control the amount of inflow of the particle size distribution adjusting gas. It is a control damper. As a result, without consuming utilities such as air and gas,
The flow rate of the particle size distribution adjusting gas can be adjusted only by rotating the gas inflow control damper 51. Here, as the gas inflow control damper, a damper made of ceramic, castor steel, or the like having excellent heat resistance and wear resistance is used, and the rotation is controlled by the particle size distribution control means by hydraulic pressure or air pressure.

(Embodiment 6) FIG. 6 is a schematic diagram of a main part of a particle size distribution adjusting tube according to Embodiment 6 of the present invention. FIG.
2a is a combustion gas flow path, 3 is a coarse dust removing device, 4a
Is a coarse dust gas passage, and 21 is a boiler top manifold, which is the same as that of the second embodiment, and therefore, is denoted by the same reference numerals and description thereof is omitted. 9d is a particle size distribution adjusting tube, 61
Is one or more control valves disposed in the particle size distribution adjusting pipe 9d. This allows the user to simply open and close the control valve 61 without consuming utilities such as air and gas.
The flow rate of the particle size distribution adjusting gas can be optimally controlled. Here, as the control valve 61, a valve made of vester cast steel, Inconel, or the like is used, and its opening and closing are controlled by hydraulic pressure, air pressure, and the like.

(Embodiment 7) FIG. 7 is a schematic view of a main part of a particle size distribution adjusting tube according to Embodiment 7 of the present invention. FIG.
Reference numeral 2b denotes a combustion gas flow path, 3 'denotes a coarse dust removal device comprising one or a plurality of cyclones arranged side by side in a boiler top manifold (not shown), 4b denotes a coarse dust gas discharge flow path, 71 Is a small-diameter particle size distribution adjusting pipe branched from the combustion gas flow path 2b to each coarse dust removal device and connected to the coarse dust removal gas discharge flow path 4b. Thereby, the coarse dust removing device 3 '
Ash dust with a large particle diameter in the gas flowing into
Has the function of adjusting the particle size distribution of ash dust flowing into the precision dust removing device. In addition, it is possible to adjust the particle size distribution without significantly changing the layout of existing cyclones, and because the piping is small and lightweight, it is excellent in workability such as installation and replacement. Having. Here, the small-diameter particle size distribution adjusting pipe 71 provided for each of one or a plurality of cyclones is set to have a gas amount of 8 to 50% of the gas amount flowing into each cyclone. It is preferable to design so as not to cause a difference between the two. In addition, a valve may be provided in the small diameter particle size distribution adjusting pipe 71 to adjust the gas flow rate. This is because there is no deviation in the performance and wear of the cyclone.

(Embodiment 8) FIG. 8 is a schematic diagram of a main part of a particle size distribution adjusting pipe disposed in a circulating pressurized fluidized-bed boiler according to Embodiment 8 of the present invention. In FIG. 8, reference numeral 81 denotes a circulating pressurized fluidized-bed boiler having a superficial velocity of 5 to 7 m / s;
a is a heat transfer tube disposed inside the circulating pressurized fluidized-bed boiler 81, 82 is a combustion gas flow path, 83 is a coarse dust removing device composed of a cyclone or the like, and 83a is a circulating pressurizing fluid from the coarse dust removing device 83. A dust circulating unit for circulating ash dust in the fluidized bed of the floor boiler 81; 84, a coarse dust removal gas discharge channel discharged from the coarse dust removal device 83; 81b, a boiler top; 85, a particle size distribution adjusting pipe;
86 is an orifice. Embodiment 1 is Embodiment 1.
8 is different from that of the first embodiment in that the pressurized fluidized-bed boiler 81 is of a circulation type and the superficial velocity in the fluidized bed is 5 to 7 m / s.
The point is that a particle size distribution adjusting tube 85 provided with an orifice 86 is provided at the boiler top 81b and communicates with the coarse dust gas flow path 84. As a result, the ash dust, which has been coarsely evacuated from the coarse dust removing device 83, is returned to the circulating pressurized fluidized bed, so that the ash dust can be made larger in particle size. ) Has the effect of adjusting the particle size distribution of the ash dust flowing into the ash dust. In addition, since ash dust containing unreacted calcium oxide that has not been consumed in the circulating pressurized fluidized-bed boiler 81 can be circulated and effectively used, the desulfurization effect can be further improved.

[0022]

Next, the present invention will be described in detail with reference to comparative examples and examples. (Comparative Example 1) Various measurements were performed using a 71 MW pressurized fluidized-bed power generation system equipped with seven cyclones (dust removal efficiency: about 90%) as the coarse dust remover 3 and two ceramic tube filters as the fine dust remover 5. Was done. At 100% load, the boiler outlet gas has a bed temperature of 860 ° C and a gas pressure of 11 kg / c.
m ² g, the average particle size of the contained ash dust was 15 to 20 μm, the maximum was 300 μm, and the content was 28.8 g / Nm ³ . The temperature of the gas flowing into the ceramic tube filter via the cyclone is 850 ° C, and the gas pressure is 9 kg / cm
^The content of ² g and ash dust was 1 g / Nm ³ . The relationship between the particle size and the amount of trapped ash dust in the ceramic tube filter was measured, and the results are shown in FIG. Thereby, the particle size is about 0.5 μm to 20 μm, the average particle size is 2 to 3 μm,
It can be seen that particles having a small particle size are concentrated, and the width of the particle size distribution is narrow. Since the particle size of the ash dust flowing into the ceramic tube filter is small and the width of the particle size distribution is narrow, ash easily adhered to the ceramic tube filter, and the pressure loss was about 3000 mmAq. For this reason, it was found that the backwashing had to be performed at intervals of 9 minutes, and even when the operation was performed for about two weeks, the ceramic tube filter was clogged.

(Example 1) In the same 71 MW pressurized fluidized bed power generation system as in the comparative example, a particle size distribution adjusting pipe was provided from the top of the pressurized fluidized bed boiler to the coarse dust gas flow path, and the particle size distribution was adjusted by an orifice. The use gas flow rate was set to be 8% of the total amount of the dust-containing gas, and the relationship between the particle size and the amount of trapped ash dust in the ceramic tube filter was measured. The results are shown in FIG. According to this, as in the particle size distribution chart of Comparative Example 1, there is a small peak due to ash dust having a particle size of 10 μm or less, but a large peak is newly formed around a particle size of approximately 50 μm, and the particle size distribution is significantly expanded. I knew it was there. The average particle size of the ash dust was about 6 μm, and the maximum particle size was about 100 μm. The ash dust content flowing into the ceramic tube filter is about 2 g /
Nm ³ , which was about twice as large as that of the comparative example in which the particle size distribution adjusting tube was not provided. By providing the particle size distribution adjusting tube in this manner, it can be seen that ash dust having a large particle size is selectively mixed with the coarse dust gas and flows into the ceramic tube filter. As a result, the pressure loss as a system with a ceramic tube filter is 2800
mmAq, and it was found that the pressure loss can be reduced by about 7% as compared with Comparative Example 1 without the particle size distribution adjusting tube. It was found that the pressure loss hardly changed even if the backwashing was performed once every 12 minutes, and the pressure loss was stable at about 2900 mmAq even once every 24 minutes. It has been confirmed that the pressurized fluidized-bed boiler operates stably without being largely affected by the increase or decrease of the combustion gas. Further, even after one month of continuous operation, no ash dust adhered or clogged in the ceramic tube filter, and it was confirmed that stable operation was possible for a long period of time.

Example 2 In the same system as in Example 1, the orifice plate was removed, and the gas flow rate for adjusting the particle size distribution was set to be 12% of the total amount of the dust-containing gas. As a result, as shown in FIG. 9, the relationship between the particle size of the ash dust flowing into the ceramic tube filter and the amount of captured ash dust was determined in Example 1.
The flow rate of the gas for adjusting the particle size distribution in the case of
Furthermore, it was found that the ash dust having a large particle diameter increased. The average particle size of the ash dust is 7 μm, and the maximum particle size is about 150 μm.
Met. Ash dust content increased to 3g / Nm ³ but pressure loss at ceramic tube filter was 2600mmA
q, which is 1 compared to the case without the particle size distribution adjusting tube.
It has been found that the pressure loss can be reduced by 3% or more. Backwashing can be performed once every 12 minutes without substantially changing the pressure loss amount, and even when performed once every 24 minutes, the pressure loss is 2700 to 2900 mm.
It was confirmed that it was stable between Aq. Also, 30
It has been found that even at intervals of one minute, operation can be performed with almost the same pressure loss. Further, by extending the backwashing interval, the consumption of high-pressure air for backwashing can be reduced, and the operation of the compressor for high-pressure air can be reduced from two to one.
It has been found that the number can be reduced to the number of stations, and the in-house rate can be improved by 0.5%. In addition, it was confirmed that the operation of the pressurized fluidized-bed boiler was stable with almost no influence of the change in the combustion gas due to the change in the combustion state. In addition, it was confirmed that no clogging or blockage due to the adhesion of ash dust on the inner surface of the ceramic tube filter occurred even after one month of continuous operation.

Comparative Example 2 (Examples 3 and 4) Next, the relationship between the particle size of ash dust and the amount of trapped ash dust was measured for the ceramic tube filter under a 50% load.
The results are shown in FIG. As is apparent from FIG. 10, the same result was obtained even when the load was 50%.

[0026]

According to the dust removing device for dust-containing high-temperature and high-pressure gas according to claim 1 of the present invention, a. The provision of a particle size distribution adjusting tube broadens the particle size distribution of the ash dust flowing into the precision dust removal device and increases the amount of coarse ash dust particles, so that ash dust adheres to the precision dust removal device such as a ceramic tube filter. Since the pressure loss can be reduced and the pressure loss can be reduced, the efficiency of power generation and the like can be increased. b. Further, the thermal stress on the precision dust removing device such as a ceramic tube filter can be reduced, and the frequency of backwashing can be reduced, so that the durability and reliability of the precision dust removing device can be improved. c. Since the frequency of backwashing can be reduced, the internal rate can also be reduced, and the efficiency of power generation and the like can be improved.

According to the dust-removing device for dust-containing high-temperature and high-pressure gas according to the second aspect of the present invention, in addition to the effect of the first aspect, the particle size distribution adjusting tube is provided with a dust-containing high-temperature and high-pressure gas generating device. Since it is provided between the top and the coarse dust gas flow path, the particle size distribution adjusting tube can be shortened, so it is effective without losing the flow rate and heat of the particle size distribution adjusting gas flowing through the particle size distribution adjusting tube. The particle size distribution of the ash dust flowing into the precision dust removing device can be adjusted.

According to the dust-containing high-temperature and high-pressure gas dedusting apparatus according to claim 3 of the present invention, a. Even in a dust-containing high-temperature and high-pressure gas generator such as a circulating fluidized bed with a superficial velocity of 5 to 7 m / s, it is possible to adjust the particle size distribution of ash dust flowing into the precision dust remover. Can be reduced, and stable operation can be achieved. b. In addition, since the ash dust containing unreacted calcium oxide that has not been consumed in the dust-containing high-temperature and high-pressure gas generator can be effectively used, such as circulating, the desulfurization effect in the dust-containing high-temperature and high-pressure gas generator is improved. be able to.

According to the method for removing dust-containing high-temperature and high-pressure gas according to claim 4 of the present invention, any one of claims 1 to 3 is provided.
In addition to the effect of the invention described in the paragraph, the particle size distribution can be controlled from the degree of clogging detected by the degree of clogging detection in the precision dust removal device, so that the load on the precision dust removal device is reduced. It can be reduced and set optimally. Further, when clogging occurs due to a rapid change in the combustion state, the clogging can be eliminated by adjusting the particle size distribution.

According to the method for removing dust-containing high-temperature and high-pressure gas according to claim 5 of the present invention, a. Since the particle size distribution of the ash dust flowing into the precision dust removal device expands and the amount of coarse ash dust particles increases, the adhesion of ash dust to the precision dust removal device such as a ceramic tube filter decreases, and the pressure loss can be reduced. Therefore, the efficiency of power generation and the like can be improved. b.
Since the thermal stress on the precision dust removal device can be reduced and the backwashing time, frequency and pressure can be reduced,
The durability and reliability of the ceramic tube filter can be improved. c. Since the backwashing time, frequency, and pressure can be reduced, the in-house ratio and utility can be reduced, and the efficiency of power generation and the like can be improved.
d. Even if the operation is performed for a long period of time, the ceramic tube filter is less likely to be blocked by ash dust and the amount of generated stress is reduced, so that accidents such as breakage can be prevented.

According to the dust removing method for dust-containing high-temperature and high-pressure gas described in claim 6 of the present invention, in addition to the effects of the invention described in claim 5, a. It is possible to adjust the particle size distribution of the ash dust flowing into the precision dust removing device by adapting to the particle size distribution of the ash dust that varies depending on the type of coal and changes in the combustion state. b. An optimal dust removal method can be provided by controlling the amount of gas and the amount of ash dust passing through the particle size distribution adjusting tube in the above range according to a sudden change in the combustion state.

[Brief description of the drawings]

FIG. 1 is a schematic diagram of a main part of a dust removing device according to a first embodiment of the present invention.

FIG. 2A is a schematic diagram of a main part of a particle size distribution adjusting tube according to a second embodiment of the present invention. FIG. 2B is a schematic diagram of a main part of a particle size distribution adjusting tube according to a second embodiment of the present invention.

FIG. 3 is a schematic diagram of a main part of a particle size distribution adjusting tube according to a third embodiment of the present invention.

FIG. 4 is a schematic diagram of a main part of a particle size distribution adjusting tube according to a fourth embodiment of the present invention.

FIG. 5 is a schematic diagram of a main part of a particle size distribution adjusting tube according to a fifth embodiment of the present invention.

FIG. 6 is a schematic diagram of a main part of a particle size distribution adjusting tube according to a sixth embodiment of the present invention.

FIG. 7 is a schematic diagram of a main part of a particle size distribution adjusting tube according to a seventh embodiment of the present invention.

FIG. 8 is a schematic diagram of a main part of a particle size distribution adjusting tube disposed in a circulating pressurized fluidized bed boiler according to an eighth embodiment of the present invention.

FIG. 9 is a graph showing the relationship between the amount of ash trapped in a ceramic tube filter and the particle size under a 100% load.

FIG. 10 is a graph showing the relationship between the amount of ash trapped in a ceramic tube filter and the particle size under a 50% load.

FIG. 11 is a schematic diagram of a main part of a conventional pressurized fluidized bed combined cycle system.

FIG. 12 is a sectional view of a main part of the precision dust removing device.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Dust-containing high-temperature and high-pressure gas generator 1a Heat transfer tube 2, 2a Combustion gas flow path 3, 3 'Coarse dust removal device 4, 4a Coarse dust removal gas passage 4b Coarse dust removal gas discharge passage 5 Precision dust removal device 6 Clean Gas flow path 7 Gas turbine 8 Generator 9, 9a, 9a ', 9b, 9c, 9d Particle size distribution adjusting tube 11 Pressure vessel 12 Ceramic tube filter 13 Top chamber 14a, 14b, 14c, 14d Support plate 15a, 15b, 15c Removal Dust chamber 16 Hopper 17a, 17b, 17c Ejector 18a, 18b, 18c Backwash nozzle 19a, 19b, 19c High-speed backwash valve 20a, 20b, 20c Backwash air inflow passage 21 Boiler top manifold 22 Gas extraction part for particle size distribution adjustment 23 Orifice 31 Particle Size Distribution Adjustment Gas Outlet 32 Gas Injector 32a Gas Inlet 33 Control Valve 34 Particle Size Distribution Control Means 41a, 41b Gas Injector 42a, 42b Control Valve 51 Gas Inflow Control Damper 61 Control Valve 71 Small Diameter Particle Size Distribution Adjusting Tube 81 Circulating Pressurized Fluidized Bed Boiler 81a Heat Transfer Tube 81b Boiler Top 82 Combustion Gas passage 83 Coarse dust removal device 83a Ash dust circulation section 84 Coarse dust removal gas discharge passage 85 Particle size distribution adjusting tube 86 Orifice

──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. ⁶ Identification code FI B01D 50/00 502 B01D 50/00 502Z 51/02 51/02

Claims (6)

[Claims] 1. A coarse dust removing device for roughly removing dust-containing high temperature and high pressure gas generated by a dust containing high temperature and high pressure gas generator, and a precision dust removing device for precisely removing coarsely dusted gas. A dust-removing device for dust-containing high-temperature and high-pressure gas, comprising a particle size distribution adjusting tube for adjusting the particle size distribution of ash dust in the gas flowing into the precision dust removing device, a combustion gas channel and a coarse dust gas channel. A dust-removing device for dust-containing high-temperature and high-pressure gas, provided in between. 2. A coarse dust remover for roughly removing dust-containing high-temperature and high-pressure gas generated by a dust-containing high-temperature and high-pressure gas generator, and a precision dust remover for precisely removing coarsely-dusted gas. A dust-removing device for dust-containing high-temperature and high-pressure gas, comprising a particle size distribution adjusting pipe for adjusting the particle size distribution of ash dust in the gas flowing into the precision dust removing device; A dust removing device for dust-containing high-temperature and high-pressure gas, which is provided between coarse dust removing gas passages. 3. A coarse dust removing device for roughly removing dust-containing high-temperature and high-pressure gas generated by a dust-containing high-temperature and high-pressure gas generator, and a precision dust removing device for precisely removing coarsely-dusted gas. A dust-removing device for dust-containing high-temperature and high-pressure gas, wherein an ash-dust circulating unit that circulates ash dust removed by the coarse dust-removing device to the dust-containing high-pressure and high-pressure gas generator, and a top of the high-temperature and high-pressure gas generator A particle size distribution adjusting pipe connected between the gas flow path and the coarse dust removal gas flow path and configured to adjust the particle size distribution of ash dust in the gas flowing into the precision dust removal device. Dust removal device for high temperature and high pressure gas. 4. A particle size distribution for controlling a particle size distribution of fine ash dust particles in a gas based on a degree of clogging detected by the precision dust removing device, and a degree of clogging detected by the degree of clogging detected by the degree of clogging. 2. A control means, comprising:
The dust removing device for dust-containing high-temperature and high-pressure gas according to any one of Items 1 to 3. 5. A coarse dust removing step in which the dust-containing high-temperature high-pressure gas generated from the dust-containing high-temperature high-pressure gas generator passes through a coarse dust removing device, and a coarse dust removing gas passes through a precision dust removing device. A dust-removing high-temperature and high-pressure gas, comprising: a precision dust-removing step of performing precise dust removal, wherein a part of the dust-containing high-temperature and high-pressure gas generated from the dust-containing high-temperature and high-pressure gas generator has a particle size distribution. A method for removing dust-containing high-temperature and high-pressure gas through a regulating pipe and flowing into the precision dust removing device. 6. The dust-containing high-temperature and high-pressure gas amount passing through the particle size distribution adjusting tube is 1 to 95%, preferably 3 to 85%, more preferably 8 to 50% of the total dust-containing high-temperature and high-pressure gas amount. The method for removing dust-containing high-temperature and high-pressure gas according to claim 5.