WO2019107422A1 - 流動床監視方法及び装置 - Google Patents
流動床監視方法及び装置 Download PDFInfo
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- WO2019107422A1 WO2019107422A1 PCT/JP2018/043806 JP2018043806W WO2019107422A1 WO 2019107422 A1 WO2019107422 A1 WO 2019107422A1 JP 2018043806 W JP2018043806 W JP 2018043806W WO 2019107422 A1 WO2019107422 A1 WO 2019107422A1
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- fluidized bed
- flow
- ratio
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
- F23C10/30—Control devices specially adapted for fluidised bed, combustion apparatus for controlling the level of the bed or the amount of material in the bed
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- the present invention relates to a technique for monitoring the condition of a fluidized bed of a fluidized bed furnace.
- a fluidized bed furnace in which a fluidized bed is formed in which a fluidized medium filled in the lower part of the furnace is made to flow with a flowing gas blown from a furnace bottom.
- a fluidized bed furnace generally, it is not possible to visually confirm the state of the fluidized bed in operation. Therefore, a technology has been proposed for detecting the state of the fluidized bed using a sensor or the like during operation of the fluidized bed furnace.
- Patent Document 1 two or more pressure sensors are disposed at different positions in the depth of the fluidized bed along the furnace inner wall surface, and the height of the fluidized bed is measured based on the measurement values obtained by these pressure sensors. Detecting levels is described.
- Patent Document 2 pressure extraction holes are provided at two points of different height in the fluidized bed, and the pressure difference between the two points is measured, and the particle shape of the fluid material is obtained from the temporal change of those values. Indirect prediction of the increase (deterioration) of is described.
- Patent Document 3 a plurality of temperature sensors distributed in the depth direction in the fluidized bed and a plurality of temperature sensors distributed in the arranging direction of the wind box arranged in the lower part of the furnace It is described that a temperature sensor is provided, and a localized flow failure site of the fluidized bed is specified from the temperature distribution obtained from the temperature sensor.
- the fuel is partially burned (gasified) in the fluidized bed with the air ratio in the fluidized bed being a low air ratio condition of 0.2 to 0.6, for example.
- the air ratio in the fluidized bed being a low air ratio condition of 0.2 to 0.6, for example.
- unburned carbon unburned carbon
- the specific gravity of the unburned char is smaller than the specific gravity of the fluid medium (eg, silica sand), so when the proportion of unburned char in the fluidized bed increases, the volume of the fluidized bed expands and the density decreases, and the flow characteristics May deteriorate.
- a mixture of a plurality of materials including silica sand and an anticoagulant comprising a material (a porous material such as zeolite or calcium oxide) that absorbs an alkali component of silica sand is used as a fluid medium.
- a material a porous material such as zeolite or calcium oxide
- the proportion of the anticoagulant in the fluidized bed becomes excessive, the volume of the fluidized bed expands to reduce the density, which may deteriorate the flow characteristics.
- the present invention proposes an apparatus and method for monitoring the rate of flow inhibition factor contained in the fluidized bed of the fluidized bed furnace.
- a fluidized bed furnace in which a fluidized bed formed by flowing a fluidized medium filled in a lower part of a furnace with a gas for flowing out from a furnace bottom is formed.
- a fluid bed monitoring method for monitoring conditions comprising: Defining a segment in the height direction in the fluidized bed and detecting a pressure difference between the upper end level and the lower end level of the segment; Based on the detected pressure difference, a ratio of a flow inhibition factor contained in the segment to reduce the fluidity of the fluid bed by reducing the density of the fluid bed is determined. It is characterized in that the ratio of the flow inhibiting factor is monitored during operation of the fluidized bed furnace.
- the flow is The percentage of inhibitory factor can be determined.
- a fluidized bed monitoring apparatus is the fluidized bed furnace in which a fluidized bed is formed in which a fluidized medium filled in the lower part of the furnace is made to flow with a flowing gas blown out from the furnace bottom.
- a fluidized bed monitoring device for monitoring the condition of the bed comprising A segment in the height direction is defined in the fluid bed, A pressure sensor provided on the inner wall of the fluidized bed furnace in contact with the fluidized bed to detect a pressure difference between the upper end level and the lower end level of the segment;
- a calculation unit for determining a ratio of a flow inhibiting factor which reduces the fluidity of the fluid bed by reducing the density of the fluid bed contained in the segment based on the detected pressure difference;
- a monitoring unit that monitors the rate of the flow inhibiting factor during operation of the fluidized bed furnace.
- the calculation unit may set a pressure difference reference value, which is a pressure difference between the upper end level and the lower end level of the segment in a state where fuel is not supplied to the fluidized bed, and the detected pressure difference. From the difference, the ratio of the flow inhibition factor can be determined.
- the above fluid bed monitoring method and apparatus it is possible to monitor the rate of flow inhibiting factors such as unburned carbon (including unburned char) in the fluid bed during operation of the fluid bed furnace. And based on the change of the ratio of the flow inhibiting factor in the fluidized bed, it is possible to predict the deterioration of the flow characteristics of the fluid bed caused by the increase of the ratio of the flow inhibiting factor in the fluidized bed. This allows appropriate treatment to take place before the flow characteristics of the fluidized bed are degraded to avoid deterioration of the flow characteristics of the fluid bed.
- unburned carbon including unburned char
- the ratio of the flow inhibiting factor is determined in two or more segments having different height levels, and the ratio of the flow inhibiting factor in two or more of the segments is monitored during operation of the fluidized bed furnace You may
- the calculation unit determines the ratio of the flow inhibition factor in two or more segments having different height levels, and the monitoring unit determines whether the fluidized bed furnace is in operation 2.
- the ratio of the flow inhibition factor in the above segments may be monitored.
- predetermined processing when an increase in the ratio of the flow inhibiting factor locally in the fluidized bed is observed from the ratio of the flow inhibiting factors of two or more of the segments, predetermined processing may be performed.
- the monitoring unit determines that the ratio of the flow inhibiting factor locally in the fluidized bed is found from the ratio of the flow inhibiting factors of the two or more segments. You may process it.
- the deterioration of the fluid flow characteristics of the fluid bed is prevented by detecting an increase in the rate of the local fluid flow inhibition factor in the fluid bed and taking action according to the situation. Can.
- a predetermined treatment may be performed when an increase in the proportion of the flow inhibiting factor as a whole of the fluidized bed is observed from the proportions of the flow inhibiting factors of two or more of the segments.
- the monitoring unit determines that the ratio of the flow inhibiting factors of the fluid bed is generally increased from the ratio of the flow inhibiting factors of the two or more segments. You may process it.
- FIG. 1 is a block diagram showing a schematic configuration of a combustion system including a fluidized bed furnace according to an embodiment of the present invention.
- FIG. 2 is a view showing a schematic configuration of a fluidized bed furnace according to an embodiment of the present invention.
- FIG. 3 is an enlarged view of the fluidized bed portion of the fluidized bed furnace.
- FIG. 4 is a diagram showing the configuration of a fluidized bed monitoring device.
- FIG. 5 is a chart showing the relationship between unburned carbon concentration and differential pressure in a certain segment.
- combustion system 100 First, the configuration of a combustion system 100 including a fluidized bed furnace 1 according to an embodiment of the present invention will be described.
- the combustion system 100 shown in FIG. 1 is a system that burns fuel (combustion target) such as coal, biomass, RDF, municipal waste, and industrial waste, and recovers its exhaust heat.
- fuel combustion target
- FIG. 1 is a system that burns fuel (combustion target) such as coal, biomass, RDF, municipal waste, and industrial waste, and recovers its exhaust heat.
- the combustion system 100 comprises a fluidized bed furnace 1 for burning fuel.
- the flue gas system 3 of the fluidized bed furnace 1 is provided with a heat exchange device 31, a cyclone dust collector 32, a bag filter 33, and an induction blower 34 which is an induction fan. Exhaust heat from the fluidized bed furnace 1 is recovered by the heat exchanger 31 and dust is separated by the cyclone type dust collector 32 and the bag filter 33, and a part thereof is discharged out of the system through a chimney not shown by the induction blower 34. Be done.
- An exhaust gas recirculation system 4 is connected to the downstream side of the bag filter 33 of the combustion exhaust gas system 3.
- a gas recirculation blower 40 is provided in the exhaust gas recirculation system 4, and a part of the combustion exhaust gas of the combustion exhaust gas system 3 is returned to the fluidized bed furnace 1 by the gas recirculation blower 40.
- the flue gas returned to the fluidized bed furnace 1 by the flue gas recirculation system 4 is used as a fluidizing gas (primary combustion gas), a secondary combustion gas, and a tertiary combustion gas.
- the fluidized bed furnace 1 shown in FIG. 2 is an operation control device for controlling the operation of the fluidized bed furnace 1 and a furnace main body 10 provided with a combustion chamber consisting of a fluidized bed portion 11 at the lower part of the furnace and a freeboard portion 12 above it. And a fluidized bed monitoring device 9.
- a throttle portion 13 At the lower portion of the freeboard portion 12, there is a throttle portion 13 in which the gas passage cross-sectional area is narrowed as compared with the remaining portion of the combustion chamber.
- the combustion gas flows upward from the bottom, and in the flue connected to the upper portion of the freeboard portion 12, a heat transfer pipe constituting the heat exchange device 31 is installed.
- FIG. 3 is an enlarged view of the fluidized bed portion 11.
- the fluidized bed 11 is filled with a fluidized bed 51 filled with a fluidized medium such as silica sand, and a fluidizing gas supply device 52 for supplying a fluidizing gas to the fluidized bed 51 from its bottom.
- An internal circulating fluidized bed is formed by the partition walls 41 and 42 which divide the fluidized bed 51 into three cells 61, 62 and 63.
- the first partition wall 41 divides the lower portion of the furnace main body 10 including the fluidized bed portion 11 into a combustion area 53 and a heat recovery area 54.
- the second partition wall 42 is provided close to the first partition wall 41 and in parallel with the first partition wall 41 in the heat recovery region 54.
- the fluidized bed portion 11 is formed by the partition walls 41 and 42 between the first side wall 10 a of the furnace main body 10 and the first partition wall 41, the “combustion cell 61”, the first partition wall 41 and the second Three cells of “circulating cell 62” formed between partition wall 42 and “heat collecting cell 63” formed between second partition wall 42 and second side wall 10 b of furnace main body 10 It is divided.
- the heat collection cell 63 is provided with a heat transfer pipe 64 such as a superheater pipe or an evaporator pipe. Heat recovery is performed by the heat medium passing through the heat transfer tube 64.
- a combustion chamber extending linearly in the vertical direction is formed above the combustion area 53.
- a ceiling wall 43 closing the upper portion of the heat recovery area 54 is provided above the heat recovery area 54.
- the upper end of the first partition wall 41 is close to the ceiling wall 43, and an upper communication port serving as an unburned gas supply port 68 is formed between the upper end of the first partition wall 41 and the ceiling wall 43.
- the lower end of the first partition wall 41 is higher than the lower end of the second partition wall 42, whereby a lower communication port 55 through which the fluid medium flows is formed in the lower portion of the first partition wall 41.
- communication ports 56, 57 are formed, which communicate the circulation cell 62 with the heat collecting cell 63 and through which the fluid medium flows.
- the flow gas supply device 52 supplies the flow gas whose flow rate is independently adjusted to each of the combustion cell 61, the circulation cell 62, and the heat collection cell 63.
- one or a plurality of air diffusers 80 having a large number of blowout ports opened to the side are provided.
- Each aeration tube 80 is disposed below the lower ends of the first partition wall 41 and the second partition wall 42.
- the flow gas supply device 52 includes a wind box disposed at the bottom of each of the cells 61, 62, 63, and a gas dispersion plate provided to close the top of the wind box. You may have (all are not shown).
- the air diffusion pipe 80 is connected by a header for each of the cells 61, 62, 63, and each header is a flow provided with flow rate adjusting means 81a, 82a, 83a such as a damper (or valve) and flowmeters 81b, 82b, 83b.
- the gas supply pipes 81, 82, 83 are connected.
- Air is supplied by the pushing blower 79.
- an exhaust gas recirculation system 4 is connected to a flow gas supply pipe 83 connected to the air diffusion pipe 80 disposed at the bottom of the heat collection cell 63.
- the operation control device 15 supplies gas for flow based on detection values of temperature sensors (not shown) for detecting the temperatures of the combustion cells 61 and the heat collecting cells 63 in the fluidized bed 51 and the flowmeters 81b, 82b, 83b, etc.
- the flow rate adjusting means 81a, 82a, 83a are operated to adjust the flow rate of the flowing gas in the pipes 81, 82, 83. From the bottom of the combustion cell 61 and the circulation cell 62, air is blown out as a flow gas, and from the bottom of the heat collection cell 63, combustion exhaust gas is blown out as a flow gas.
- the superficial velocity of the flowable gas of the combustion cell 61 is larger than the superficial velocity of the flowable gas of the heat collection cell 63, and the superficial velocity of the flowable gas of the circulation cell 62 is equal to that of the combustion cell 61.
- the flow rate of the flowable gas is adjusted to be greater than the superficial velocity of the flowable gas and the superficial velocity of the flowable gas of the heat collection cell 63.
- the flow of the fluid medium occurs such that the fluid medium of the heat collection cell 63 is circulated to the combustion cell 61 and the circulation cell 62 through the lower communication port 57 of the second partition wall 42 after moving to the heat collection cell 63.
- the heat energy of the flowable medium having a high temperature in the combustion cell 61 is extracted to the outside in the heat collection cell 63, and the flowable medium having the lowered temperature is returned to the combustion cell 61.
- the temperature rise of the fluid medium of the combustion cell 61 is suppressed.
- a fuel inlet 65 is opened immediately above the surface layer portion of the fluidized bed portion 11 at the time of operation and in the first side wall 10a.
- the fuel inlet 65 is located on the upstream side of the flow of the combustion gas than the throttle portion 13.
- Fuel is supplied to the fuel inlet 65 by a fuel supply device (not shown). The fuel introduced into the furnace from the fuel inlet 65 falls to the top of the combustion cell 61 of the fluidized bed portion 11.
- an unburned gas supply port 68 is opened. From the unburned gas supply port 68, the mixture of air and combustion exhaust gas which is blown out from the aeration pipe 80 disposed in the fluidized bed 51 of the heat recovery area 54 into the fluidized bed 51 and passes through the fluidized bed 51 , As a secondary combustion gas.
- a supply port for blowing out the secondary combustion gas may be provided.
- a plurality of tertiary combustion gas supply ports 69 are opened in the furnace wall on the downstream side of the flow of the combustion gas than the unburned gas supply port 68.
- the plurality of tertiary combustion gas supply ports 69 are provided to be dispersed at a plurality of height positions.
- a temperature sensor 70 is provided on the furnace wall included in the diffusion area of the tertiary air blown out from the tertiary combustion gas supply port 69.
- the air content of the tertiary combustion gas is adjusted by mixing the combustion exhaust gas with air.
- flow control means 88, 89 such as dampers (or valves) are provided in the air supply path to the tertiary combustion gas supply port 69 and the combustion exhaust gas supply path.
- the operation control device 15 maintains the flow rate of the tertiary combustion gas at the predetermined flow rate, and supplies the tertiary combustion gas to that point.
- the flow rate adjusting means 88, 89 so that the air content of the tertiary combustion gas supplied to that point is increased. Adjust the opening of the.
- the operation method of the fluidized bed furnace 1 of the said structure is demonstrated.
- low air ratio combustion is performed in the fluidized bed portion 11. More specifically, while the total air ratio between the fluidized bed portion 11 and the freeboard portion 12 is set to a value larger than 1, the air ratio (i.e., the primary air ratio) of the combustion cells 61 of the fluidized bed portion 11 and the fuel injection
- the air content is adjusted.
- the primary air ratio is lower than the secondary air ratio.
- the primary air ratio may be 0.4 and the secondary air ratio may be 0.8.
- the slow drying and thermal decomposition of the fuel generate combustible pyrolysis gas and pyrolysis residue.
- Pyrolysis residue and fuel residue are at the bottom of the combustion cell 61, and are provided at the intermediate position between the first side wall 10a and the first partition wall 41 from the outlet 72 of the fluid medium and the incombustible material. It is discharged outside.
- the pyrolysis gas produced in the fluidized bed portion 11 is burned with the secondary combustion gas, and the unburned portion in the combustion gas is completely burned with the tertiary combustion gas in the freeboard portion 12, and the combustion exhaust gas is the combustion exhaust gas Discharged to system 3.
- the unburned content of the fuel in the combustion cell 61 (unburned char) compared to the case where the air ratio is 1 or more.
- the percentage of is large.
- the ratio of unburned char in the combustion cell 61 is particularly high as compared with the case where the conventional air ratio is about 0.8 to 0.9. growing.
- the proportion of unburned char in the combustion cell 61 increases, the density of the unburned char is lower than that of the fluid medium, so the density of the fluidized bed 51 decreases.
- the density of the fluidized bed 51 decreases, the volume of the fluidized bed 51 may expand and the flow characteristics may be deteriorated.
- unburned char may flow into the heat collection cell 63 due to the circulation of the fluidizing medium.
- it is desirable that unburned carbon is not present in the fluidized bed 51 or the proportion thereof is extremely small.
- the fluidized bed monitoring device 9 is provided to monitor the ratio of unburned carbon (including unburned char) of the fluidized bed 51 for the combustion cell 61 and the heat collecting cell 63 of the fluidized bed 11. Treatment according to the proportion of unburned carbon. Although there may be a plurality of types of flow inhibiting factors that reduce the fluidity of the fluid bed 51 by reducing the density of the fluid bed 51, here, the ratio of unburned carbon which is one of them is monitored .
- the fluid bed monitoring device 9 and the fluid bed monitoring method performed by the device will be described in detail.
- FIG. 4 is a diagram showing the configuration of the fluidized bed monitoring device 9. In FIG. 4, one of the plurality of segments S is highlighted. As shown in FIG. 4, the fluidized bed monitoring device 9 includes a plurality of pressure sensors 91, a computing unit 92, and a monitoring unit 93.
- the plurality of pressure sensors 91 are provided on the inner wall of the fluidized bed portion 11 in contact with the fluidized bed 51 in the furnace body 10 of the fluidized bed furnace 1 and are disposed at different height levels.
- the plurality of pressure sensors 91 can measure a pressure difference between two different height levels.
- the plurality of pressure sensors 91 are arranged at equal intervals in the height direction on the furnace wall of the fluidized bed portion 11. Then, between the height levels of two pressure sensors 91 adjacent in the height direction is one segment S, and using the pressure detection value at the upper end level and the pressure detection value at the lower end level of each segment S, each segment S The pressure difference between the upper end level and the lower end level (hereinafter referred to as “the differential pressure of the segment S”) is measured.
- one or a plurality of differential pressure sensors may be used in which the differential pressure of the segment S is detected by a pair of probes arranged at the upper end level and the lower end level of the segment S.
- the operation unit 92 is a so-called computer, and includes a processor, a memory, a communication interface, and the like (all not shown), and the processor executes a predetermined program stored in the memory as an operation unit 92. Demonstrate the functions of The communication interface is controlled by the processor to receive detection signals from the plurality of pressure sensors 91 and transmit / receive data to / from the monitoring unit 93 and the like using wireless or wired communication means.
- the computing unit 92 obtains detection signals of the plurality of pressure sensors 91, and obtains a differential pressure of each segment S from detection values of the plurality of pressure sensors 91.
- the detection value of each differential pressure sensor may be acquired as the differential pressure of the segment S.
- the computing unit 92 obtains the unburned carbon ratio of the segment S from the differential pressure of the segment S.
- the unburned carbon ratio of the segment S can be expressed as a function of the differential pressure of the segment S and the flow velocity (empty velocity) of the fluidizing gas of the target cell.
- FIG. 5 is a chart showing the relationship between unburned carbon concentration [wt%] and differential pressure [kPa] in a certain segment S.
- This chart shows the relationship between the unburned carbon concentration of the segment S and the differential pressure when the flow velocity f of the fluidizing gas of the target cell is F1, F2, F3 (F1> F2> F3).
- the unburned carbon concentration [wt%] is represented by unburned carbon weight / (flowing medium weight + unburned carbon weight) ⁇ 100 in the target segment S.
- the unburned carbon concentration of the segment S decreases as the differential pressure of the segment S increases. In other words, the unburned carbon concentration of the segment S increases as the differential pressure of the segment S decreases.
- the unburned carbon content has a smaller specific gravity than silica sand, so when the unburned carbon concentration in segment S increases, the weight of the fluid medium in segment S is lower than when the unburned carbon concentration is lower. As a result, the differential pressure (differential pressure) of the segment S decreases.
- the calculation unit 92 calculates the unburned carbon concentration from the detected differential pressure of the segment S based on the relationship between the unburned carbon concentration of the segment S and the differential pressure as described above.
- the relationship between the unburned carbon concentration of the segment S and the differential pressure is previously obtained by experiment or simulation and stored in the calculation unit 92.
- Arithmetic unit 92 substitutes for the above-described method for calculating the unburned carbon ratio, and the segment S of which unburned carbon concentration is zero (that is, in a state where fuel is not supplied to fluidized bed portion 11)
- the “pressure difference reference value” which is a differential pressure is previously obtained by experiment or simulation and stored, and the unburned carbon ratio of the segment S is calculated from the difference between the detected pressure difference of the segment S and the pressure difference reference value. It may be configured to request.
- the monitoring unit 93 is a so-called computer, and includes a processor, a memory, a communication interface, and the like (all are not shown), and the processor executes a predetermined program stored in the memory to be a monitoring unit 93. Demonstrate the functions of The communication interface is controlled by the processor to transmit / receive data to / from the monitoring unit 93, the operation control device 15, etc. using wireless or wired communication means.
- the monitoring unit 93 acquires the unburned carbon ratio of each segment S determined by the calculation unit 92, and monitors the value of the unburned carbon ratio of the fluidized bed furnace 1 in operation and the change thereof. Furthermore, when a predetermined state is detected during monitoring, the monitoring unit 93 transmits a warning and its treatment to the operation control device 15.
- the monitoring unit 93 detects that the unburned carbon ratio exceeds a predetermined threshold in the segment S included in the range from the surface layer of the fluidized bed 51 to 1 ⁇ 3 of the height dimension of the fluidized bed 51, Since it is estimated that excess unburned carbon is floating in the layer 51, a signal is sent to the operation control device 15 to reduce the amount of fuel input.
- the monitoring unit 93 detects that the unburned carbon ratio exceeds a predetermined threshold in the segment S included in the range from the bottom of the fluidized bed 51 to 1/3 of the height dimension of the fluidized bed 51, the flow Since it is estimated that excess unburned carbon is stagnating in the lower part of the layer 51, a signal is sent to the operation control device 15 to increase the flow rate of the fluidizing gas. In the state where excess unburned carbon is staying in the lower part of the fluidized bed 51, there is a possibility that the fluidization gas will not be fluidized even if supplied to the fluidized bed 51, so in the above case, the monitoring unit 93 May signal the operation control unit 15 to stop the operation of the fluidized bed furnace 1.
- the segment S whose monitoring unit 93 monitors the unburned carbon ratio may be single or plural.
- the entire area in the height direction of the fluidized bed 51 may be defined as one segment S, or a plurality of continuous segments S may be defined in the height direction of the fluidized bed 51, or the fluidized bed A plurality of segments S distributed in the height direction of 51 may be defined.
- the monitoring unit 93 monitors the unburned carbon ratio of the fluidized bed furnace 1 in operation. It is preferable to estimate the state of the fluidized bed portion 11 by comparing the fuel carbon ratio.
- the monitoring unit 93 can detect an increase in the local unburned carbon ratio in the fluidized bed 51 by comparing the unburned carbon ratios of the two or more segments S. Thus, when an increase in the local unburned carbon ratio in the fluidized bed 51 is found, the monitoring unit 93 performs processing according to the portion where the unburned carbon ratio in the fluidized bed 51 is increased. For example, in the case where the segment S where the local unburned carbon percentage increase is found is the surface layer or a portion close to the surface layer of the fluid bed 51, the timing of the segment S rising to the surface layer of the fluid bed 51 is A signal is sent to the operation control device 15 so as to reduce the input amount.
- the monitoring unit 93 determines that the flow failure of the fluidized bed 51 is predicted. At the same time, a signal is sent to the operation control device 15 to increase the flow rate of the fluidizing gas.
- the monitoring unit 93 can detect an increase in the unburned carbon ratio across the height direction of the fluid bed 51 by comparing the unburned carbon ratios of the two or more segments S.
- the two or more segments S may be dispersed in the height direction of the fluidized bed 51 or may be continuous in the height direction of the fluidized bed 51.
- the monitoring unit 93 decreases the amount of fuel input, increases the flow rate of the fluidizing gas, increases the fluidizing medium, and A signal is sent to the operation control device 15 to perform at least one process out of the one operation stop processing group.
- the monitoring unit 93 instructs the operation control unit 15 to take measures to be taken by the operation control unit 15 in the above description, the monitoring unit 93 only transmits the estimated state of the fluid bed 51 to the operation control unit 15. You may In this case, the operation control device 15 performs processing corresponding to the estimated state of the fluid bed 51 acquired from the monitoring unit 93.
- the fluidized bed monitoring device 9 is a fluidized bed in which the fluidized bed 51 is formed by causing the fluidized medium filled in the lower part of the furnace to flow with the gas for flowing out from the furnace bottom.
- the condition of the fluidized bed 51 is monitored, and a segment S in the height direction is defined in the fluidized bed 51 and provided on the inner wall of the fluidized bed furnace 1 in contact with the fluidized bed 51,
- a pressure sensor 91 for detecting a pressure difference between the upper end level and the lower end level of the segment S
- a computing unit 92 for obtaining the unburned carbon ratio of the segment S based on the detected pressure difference
- a monitoring unit 93 for monitoring the unburned carbon ratio of the fluidized bed 51.
- the fluidized bed 51 can be read as a fluidized bed.
- the computing unit 92 is, for example, a difference between a pressure difference reference value, which is a pressure difference between the upper end level and the lower end level of the segment S in a state where fuel is not supplied to the fluidized bed 51, and the detected pressure difference. Therefore, the unburned carbon ratio can be determined.
- a segment S in the height direction is defined in the fluidized bed 51, a pressure difference between the upper end level and the lower end level of the segment S is detected, and the detected pressure Based on the difference, the unburned carbon ratio of the segment S is obtained, and the unburned carbon ratio of the fluidized bed 51 is monitored during operation of the fluidized bed furnace 1.
- the ratio of unburned carbon such as unburned char in the fluidized bed 51 can be monitored during operation of the fluidized bed furnace 1. And based on the change of the ratio of the unburned carbon in the fluidized bed 51, the deterioration of the flow characteristic of the fluidized bed 51 due to the increase of the ratio of the unburned carbon in the fluidized bed 51 can be predicted. As a result, appropriate processing can be performed before the flow characteristics of the fluidized bed 51 deteriorate, and deterioration of the flow characteristics of the fluidized bed 51 can be avoided.
- the monitoring unit 93 of the fluidized bed monitoring device 9 is configured to perform the method of monitoring the unburned carbon ratio of the fluidized bed 51 exemplified below.
- the monitoring unit 93 may be configured to perform at least one of the monitoring methods. (1) In the segment S included in the range from the surface layer of the fluidized bed 51 to one third of the height dimension of the fluidized bed 51, predetermined processing is performed when the unburned carbon ratio exceeds a predetermined threshold. (2) In the segment S included in the range of 1/3 of the height dimension of the fluidized bed 51 from the bottom of the fluidized bed 51, predetermined processing is performed when the ratio of unburned carbon exceeds a predetermined threshold.
- the flow characteristics of the fluidized bed 51 are increased due to an increase in the ratio of unburned carbon in the fluidized bed 51 It can be predicted before it gets worse. Then, by performing appropriate processing before the flow characteristics of the fluidized bed 51 deteriorate, the deterioration of the flow characteristics of the fluidized bed 51 can be avoided.
- the fluidized bed monitoring device 9 according to the present invention and the fluidized bed according to the present invention The method can be applied to detect and monitor the unburned carbon fraction of the fluid bed.
- the percentage of gasification promoting material in layer 51 may be monitored.
- an oxygen storage and release material such as ilmenite (Fe-based) and a gasification promoting material of carbon such as Ni ore as a flowable medium.
- a fluidized bed furnace using a mixture of multiple materials including, as a fluid medium, silica sand and an anticoagulant made of a material (porous material such as zeolite or calcium oxide) that absorbs the alkaline component of silica sand.
- the ratio of the anticoagulant in the fluid bed 51 may be monitored as a fluid flow inhibiting factor.
- monitoring of the proportion of the anticoagulant in the fluid bed 51 and the deterioration of the flow characteristics of the proportion of the anticoagulant are read by replacing unburned carbon with "the anticoagulant". be able to.
Abstract
Description
前記流動床内に高さ方向のセグメントを規定し、そのセグメントの上端レベルと下端レベルとの圧力差を検出し、
検出された前記圧力差に基づいて、前記セグメントに含まれる、前記流動床の密度を低下させることにより当該流動床の流動性を低下させる流動阻害因子の割合を求め、
前記流動床炉の運転中に前記流動阻害因子の割合を監視することを特徴としている。
前記流動床内に高さ方向のセグメントが規定され、
前記流動床と接触している前記流動床炉の内壁に設けられ、前記セグメントの上端レベルと下端レベルとの圧力差を検出する圧力センサと、
検出された前記圧力差に基づいて、前記セグメントに含まれる、前記流動床の密度を低下させることにより当該流動床の流動性を低下させる流動阻害因子の割合を求める演算部と、
前記流動床炉の運転中に前記流動阻害因子の割合を監視する監視部とを、備えることを特徴としている。
まず、本発明の一実施形態に係る流動床炉1を含む燃焼システム100の構成について説明する。図1に示す燃焼システム100は、石炭、バイオマス、RDF、都市ごみ、産業廃棄物などの燃料(燃焼対象物)を燃焼して、その排熱を回収するシステムである。
次に、本発明の一実施形態に係る流動床炉1の構成について説明する。図2に示す流動床炉1は、炉下部の流動床部11及びその上方のフリーボード部12からなる燃焼室が設けられた炉本体10と、流動床炉1の運転を制御する運転制御装置15と、流動床監視装置9とを備えている。フリーボード部12の下部には、燃焼室の余の部分と比較してガス通路断面積が絞られた絞り部13が存在する。フリーボード部12では、燃焼ガスが下から上に向かって流れ、フリーボード部12の上部に接続された煙道には、熱交換装置31を構成する伝熱管が設置されている。
ここで、上記構成の流動床炉1の運転方法について説明する。流動床炉1では、流動床部11において低空気比燃焼が行われる。より詳細には、流動床部11とフリーボード部12との総空気比を1よりも大きい値としながら、流動床部11の燃焼セル61の空気比(即ち、一次空気比)、及び燃料投入口65の周囲の空気比(二次空気比)がいずれも1未満の低空気比となるように、燃焼セル61への流動化空気及び二次燃焼用ガスの供給量、及び/又は、その空気含有量が調整される。望ましくは、一次空気比は、二次空気比よりも低い。例えば、流動床部11とフリーボード部12との総空気比を1.2とする場合に、一次空気比を0.4とし、二次空気比を0.8としてよい。
図4は、流動床監視装置9の構成を示す図である。図4では、複数のセグメントSのうちの1つが強調して示されている。図4に示すように、流動床監視装置9は、複数の圧力センサ91と、演算部92と、監視部93とを備えている。
(1)流動層51の表層から流動層51の高さ寸法の1/3の範囲に含まれるセグメントSにおいて、未燃炭素割合が所定の閾値を超えると、所定の処理を行う。
(2)流動層51の底から流動層51の高さ寸法の1/3の範囲に含まれるセグメントSにおいて、未燃炭素割合が所定の閾値を超えると、所定の処理を行う。
(3)2以上のセグメントSの未燃炭素割合から、流動層51における局所的な未燃炭素割合の増大がみつかると、所定の処理を行う。
(4)2以上のセグメントSの未燃炭素割合から、流動層51の全体的な未燃炭素割合の増大がみつかると、所定の処理を行う。
3 :燃焼排ガス系統
4 :排ガス再循環系統
10 :炉本体
10a :第1側壁
10b :第2側壁
11 :流動床部
12 :フリーボード部
13 :絞り部
15 :運転制御装置
31 :熱交換装置
32 :サイクロン式集塵機
33 :バグフィルタ
34 :誘引ブロワ
40 :ガス再循環ブロワ
41 :第1仕切壁
42 :第2仕切壁
43 :天井壁
51 :流動層
52 :流動用ガス供給装置
53 :燃焼領域
54 :熱回収領域
55,56,57 :連通口
61 :燃焼セル
62 :循環セル
63 :収熱セル
64 :伝熱管
65 :燃料投入口
68 :未燃ガス供給口
69 :三次燃焼用ガス供給口
70 :温度センサ
72 :抜出口
79 :押込ブロワ
80 :散気管
81,82,83 :流動用ガス供給配管
81a,82a,83a :流量調整手段
81b,82b,83b :流量計
88,89 :流量調整手段
9 流動床監視装置
91 :圧力センサ
92 :演算部
93 :監視部
100 :燃焼システム
Claims (10)
- 炉内下部に充填された流動媒体を炉底から吹き出す流動用ガスで流動させてなる流動床が形成された流動床炉において、前記流動床の状態を監視する流動床監視方法であって、
前記流動床内に高さ方向のセグメントを規定し、そのセグメントの上端レベルと下端レベルとの圧力差を検出し、
検出された前記圧力差に基づいて、前記セグメントに含まれる、前記流動床の密度を低下させることにより当該流動床の流動性を低下させる流動阻害因子の割合を求め、
前記流動床炉の運転中に前記流動阻害因子の割合を監視する、
流動床監視方法。 - 前記流動床に燃料が供給されていない状態の前記セグメントの上端レベルと下端レベルとの圧力差である圧力差基準値と、検出された前記圧力差との差から、前記流動阻害因子の割合を求める、
請求項1に記載の流動床監視方法。 - 前記流動阻害因子の割合を、高さレベルの異なる2以上の前記セグメントで求め、
前記流動床炉の運転中に2以上の前記セグメントの前記流動阻害因子の割合を監視する、
請求項1又は2に記載の流動床監視方法。 - 2以上の前記セグメントの前記流動阻害因子の割合から、前記流動床における局所的な前記流動阻害因子の割合の増大がみつかると、所定の処理を行う、
請求項3に記載の流動床監視方法。 - 2以上の前記セグメントの前記流動阻害因子の割合から、前記流動床の全体的な前記流動阻害因子の割合の増大がみつかると、所定の処理を行う、
請求項3に記載の流動床監視方法。 - 炉内下部に充填された流動媒体を炉底から吹き出す流動用ガスで流動させてなる流動床が形成された流動床炉において、前記流動床の状態を監視する流動床監視装置であって、
前記流動床内に高さ方向のセグメントが規定され、
前記流動床と接触している前記流動床炉の内壁に設けられ、前記セグメントの上端レベルと下端レベルとの圧力差を検出する圧力センサと、
検出された前記圧力差に基づいて、前記セグメントに含まれる、前記流動床の密度を低下させることにより当該流動床の流動性を低下させる流動阻害因子の割合を求める演算部と、
前記流動床炉の運転中に前記流動阻害因子の割合を監視する監視部とを、備える、
流動床監視装置。 - 前記演算部が、前記流動床に燃料が供給されていない状態の前記セグメントの上端レベルと下端レベルとの圧力差である圧力差基準値と、検出された前記圧力差との差から、前記流動阻害因子の割合を求める、
請求項6に記載の流動床監視装置。 - 前記演算部は、前記流動阻害因子の割合を、高さレベルの異なる2以上の前記セグメントで求め、
前記監視部は、前記流動床炉の運転中に2以上の前記セグメントの前記流動阻害因子の割合を監視する、
請求項6又は7に記載の流動床監視装置。 - 前記監視部は、2以上の前記セグメントの前記流動阻害因子の割合から、前記流動床における局所的な前記流動阻害因子の割合の増大がみつかると、所定の処理を行う、
請求項8に記載の流動床監視装置。 - 前記監視部は、2以上の前記セグメントの前記流動阻害因子の割合から、前記流動床の全体的な前記流動阻害因子の割合の増大がみつかると、所定の処理を行う、
請求項8に記載の流動床監視装置。
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