JP5866872B2 - Cyclone system, gasification gas generation system, and cyclone control method - Google Patents

Description

  The present invention relates to a cyclone system, a gasification gas generation system, and a cyclone control method for controlling the separation efficiency of a cyclone separator.

  2. Description of the Related Art In recent years, a technology has been developed that gasifies solid raw materials such as coal, biomass, and tire chips to generate gasified gas instead of petroleum. As a system for generating such a gasified gas, a technology (water vapor) that gasifies a solid raw material at about 700 ° C. to 900 ° C. using water vapor in a gasification furnace in which a fluid medium forms a fluidized bed. Gasification) has been developed. In a gasified gas generation system using a fluidized bed, a fluidized medium is introduced into a gasifier after being heated in a combustion field of combustion gas (combustion furnace). At this time, it is common practice to separate a fluid medium heated at a combustion field at about 1000 ° C. from combustion exhaust gas using a cyclone separator.

  The cyclone separator is a device that generates a centrifugal force by swirling the introduced mixture of solid and gas and separates a solid having a predetermined particle diameter or more by the centrifugal force. The efficiency (separation efficiency) with which a solid contained in a mixture can be separated in a cyclone separator generally depends on the flow rate of the introduced mixture. That is, the higher the flow rate of the introduced mixture, the higher the separation efficiency of the cyclone separator.

  As a technique for controlling the separation efficiency of such a cyclone separator, for example, a piston capable of opening and closing the introduction pipe by the expansion and contraction of a spring is provided in the introduction pipe of the cyclone separator, and the opening of the introduction pipe is adjusted by the piston. The technique of adjusting the flow rate of the mixture introduced into a cyclone separator by adjusting is disclosed (for example, Patent Document 1). Also disclosed is a technique for adjusting the flow rate of the mixture introduced into the cyclone separator by providing a damper capable of opening and closing the introduction pipe of the cyclone separator and adjusting the opening of the introduction pipe by the damper. (For example, patent document 2).

Japanese Patent Application Laid-Open No. 2004-97942 JP 2000-26631 A

  However, in the techniques described in Patent Document 1 and Patent Document 2 described above, a mechanical structure such as a spring and a piston or a damper is used. For this reason, when it employ | adopts for the cyclone separator installed in high temperature fields, such as about 1000 degreeC like a gasification gas production | generation system, it was necessary to use the material which has heat resistance, and the cost was high. In addition, even if a mechanical structure is used for a cyclone separator installed in a high temperature field, the sealing performance of the piston and damper cannot be maintained, the flow rate of the introduced mixture cannot be adjusted, and the cyclone separator It was difficult to control the separation efficiency.

  Therefore, the present invention provides a cyclone system, a gasification gas generation system, and a cyclone control method capable of reliably controlling the separation efficiency of a cyclone separator with a simple configuration even when used in a high temperature field. It is intended to provide.

In order to solve the above problems, a cyclone system according to the present invention is configured such that a mixture of solid and gas is introduced through an inlet, and a solid having a predetermined particle size or more is dropped through the outlet by swirling the mixture. A cyclone separator that exhausts scattered particles and gas, which are solids less than a predetermined particle size, through an exhaust port positioned vertically above the drop port, a connecting pipe connected to the dropping port, and a connection pipe A gas supply section for supplying the gas back to the cyclone separator through the dropping port by supplying gas to the connection pipe through the supply pipe, and the supply pipe is connected to the connection pipe from one end. It is a pipe inclined vertically downward as it goes to the other end .

  The cyclone system includes a scattered particle detection unit that detects the concentration of scattered particles exhausted from the exhaust port, and the gas supply unit includes a flow rate adjustment unit that adjusts the flow rate of the gas supplied to the connecting pipe. The unit may adjust the flow rate of the gas supplied to the connecting pipe according to the detection result of the scattered particle detection unit.

  The separation efficiency of a solid having a predetermined particle size or more in a cyclone separator is determined by the flow rate of the mixture at the inlet, and the inlet diameter is determined by the flow rate of the mixture at the inlet during the rated operation of the cyclone separator. The separation efficiency may be lowered by setting the gas to be the fastest and supplying the gas to the connecting pipe by the gas supply unit.

In order to solve the above problems, the gasified gas generation system of the present invention generates a gasified gas by forming a fluidized bed into a fluidized bed and gasifying the input gasified raw material with the heat of the fluidized medium. From a gasification furnace, a combustion medium in which the fluidized medium and gasification raw material residue discharged from the gasification furnace are guided, and heating the fluidization medium and burning the gasification raw material residue to produce ash, and a combustion furnace The discharged mixture of heated fluid medium, ash, and combustion exhaust gas is introduced through the inlet, and the mixture is swirled to cause a solid having a predetermined particle diameter or more to fall through the outlet and to be predetermined. subjected scattering particles and gases is the particle size less than solid, a cyclone separator for exhaust through the exhaust port located vertically above the chute, the communication tube was connected to fall opening, which is connected to a communication tube By supplying gas to the communication tube via a tube, and a gas supply unit for flowing back the gas into the cyclone separator through the chute, the supply pipe, the other end connected to the communication tube from one end It is characterized by being a tube inclined vertically downward as it goes .

  The gasification gas generation system is cooled by an indirect heat exchanger and an indirect heat exchanger that perform heat exchange between the gasification gas generated in the gasification furnace and the heat medium, thereby cooling the gasification gas. A mist separator that further cools the gasification gas and removes mist from the gasification gas, and the gas supply unit has a pressure loss value of the gasification gas in at least one of the indirect heat exchanger and the mist separator. When it is equal to or greater than a predetermined value, gas may be supplied to the connecting pipe.

  The gas supply unit has a flow rate adjusting unit that adjusts the flow rate of the gas supplied to the connecting pipe, and the flow rate adjusting unit corresponds to the pressure loss value of the gasification gas in at least one of the indirect heat exchanger and the mist separator. Thus, the flow rate of the gas supplied to the connecting pipe may be adjusted.

Another gasified gas generation system of the present invention for solving the above-described problem is that a fluidized medium is fluidized and a gasified raw material is gasified with heat of the fluidized medium to generate a gasified gas. Gasification furnace, a fluidizing medium discharged from the gasification furnace and a residue of the gasification raw material are guided, the fluidizing medium is heated and the residue of the gasification raw material is burned to generate ash, and a combustion furnace A mixture of heated fluid medium, ash, and combustion exhaust gas discharged from is introduced through the introduction port, and by swirling the mixture, solids having a predetermined particle diameter or more are dropped through the drop port, A cyclone separator that exhausts scattered particles and gas, which are solids less than a predetermined particle size, through an exhaust port located vertically above the drop port, a connecting pipe connected to the dropping port, and gas to the connecting pipe Thus, the gasification gas is cooled by exchanging heat between the gas supply unit that reversely flows the gas into the cyclone separator through the dropping port and the gasification gas generated in the gasification furnace and the heat medium. An indirect heat exchanger; and a mist separator that further cools the gasified gas cooled by the indirect heat exchanger and removes mist from the gasified gas. The flow rate adjustment unit adjusts the flow rate of the gas supplied to the connecting pipe according to the pressure loss value of the gasification gas in at least one of the indirect heat exchanger and the mist separator. It is characterized by doing.
In order to solve the above problems, the cyclone control method of the present invention is a gasification method in which a fluidized medium is fluidized and gasified raw material is gasified with heat of the fluidized medium to generate gasified gas. From the furnace, the combustion medium discharged from the gasification furnace and the residue of the gasification raw material are guided, the fluidization medium is heated and the residue of the gasification raw material is burned to generate ash, and the combustion furnace The discharged mixture of heated fluid medium, ash, and combustion exhaust gas is introduced through the inlet, and the mixture is swirled to cause a solid having a predetermined particle diameter or more to fall through the outlet and to be predetermined. A cyclone separator that exhausts scattered particles and gas, which are solids less than the particle diameter, through an exhaust port positioned vertically above the drop port, a connecting pipe connected to the dropping port, and a gas in the connecting pipe The gasification gas is cooled by exchanging heat between the gas supply unit that reversely flows the gas into the cyclone separator through the outlet and the gasification gas generated in the gasification furnace and the heat medium. A cyclone control method using an indirect heat exchanger, and a mist separator that further cools the gasified gas cooled by the indirect heat exchanger and removes mist from the gasified gas. A step of determining whether or not the pressure loss value of the gasification gas in at least one of the exchanger and the mist separator is greater than or equal to a predetermined value; and if the pressure loss value is greater than or equal to a predetermined value, the gas supply unit supplies the connection pipe And a step of supplying a gas.

  According to the present invention, it is possible to reliably control the separation efficiency of the cyclone separator with a simple configuration even when used in a high temperature field.

It is explanatory drawing for demonstrating the specific structure of a gasification gas production | generation system. It is explanatory drawing for demonstrating the example of the particle size distribution of the solid in the mixture introduce | transduced into a cyclone separator. It is explanatory drawing for demonstrating an example of a gas supply part. It is explanatory drawing for demonstrating the modification of a gas supply part. It is a flowchart for demonstrating the flow of a process of a cyclone control method. It shows the concentration of scattered particles in the exhaust gas exhausted from the exhaust port of the first cyclone separator when the gas is not supplied to the connecting pipe (comparative example) and when the gas is supplied to the connecting pipe (example). FIG.

  Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. The dimensions, materials, and other specific numerical values shown in the embodiments are merely examples for facilitating the understanding of the invention, and do not limit the present invention unless otherwise specified. In the present specification and drawings, elements having substantially the same function and configuration are denoted by the same reference numerals, and redundant description is omitted, and elements not directly related to the present invention are not illustrated. To do.

  Here, in order to grasp the purpose of the cyclone system, first, a gasification gas generation system in which the cyclone system is installed will be described, and then a specific configuration of the cyclone system according to the present embodiment will be described in detail.

(Gasified gas generation system 100)
FIG. 1 is an explanatory diagram for explaining a specific configuration of a gasification gas generation system 100 according to the present embodiment. As shown in FIG. 1, the gasification gas generation system 100 includes a gasification furnace 110, a combustion furnace 120, a cyclone system 200, a second cyclone separator 130, a reforming furnace 160, and an indirect heat exchanger 162. The spray tower 164 and the mist separator 166 are included. The cyclone system 200 includes a first cyclone separator 210, a connecting pipe 212, a gas supply unit 214, and a scattered particle detection unit 216.

  In the gasification gas generation system 100, as a whole, a fluid medium composed of sand such as dredged sand (silica sand) having a particle size of about 300 μm is circulated as a heat medium. Specifically, first, the fluid medium is heated to about 1000 ° C. in the combustion furnace 120 and introduced into the first cyclone separator 210 together with the combustion exhaust gas. In the first cyclone separator 210, the high temperature fluid medium and the combustion exhaust gas are separated, and the separated high temperature fluid medium is introduced into the gasifier 110 through the connecting pipe 212, the seal portion 102a, and the introduction portion 140a. The Then, the fluidized medium introduced into the gasification furnace 110 is fluidized by a gasifying agent (water vapor, nitrogen, inert gas, etc.) introduced from the gasifying agent storage part 112, and the discharge part 140b and the sealing part 102b. To the combustion furnace 120.

  On the other hand, the gasification gas generated in the gasification furnace 110 is separated into a fluid medium and a gasification gas in the second cyclone separator 130, and then oxidized and reformed in the reforming furnace 160, and the indirect heat exchanger 162. In the spray tower 164 and the mist separator 166, impurities such as tar are removed. Below, each apparatus which comprises the gasification gas production | generation system 100 is demonstrated concretely.

(Gasification furnace 110)
The gasification furnace 110 communicates with the first cyclone separator 210 via the introduction part 140a, the seal part 102a, and the connecting pipe 212, and the fluidized medium separated from the combustion exhaust gas by the first cyclone separator 210 is a gas. Introduced into the conversion furnace 110.

  A gasifying agent storage unit 112 is provided below the gasification furnace 110, and the gasifying agent supplied from a gasifying agent supply source (not shown) is temporarily stored in the gasifying agent storage unit 112. Is done. The gasifying agent stored in the gasifying agent storage part 112 is introduced into the gasifying furnace 110 from the bottom surface of the gasifying furnace 110. Thus, a fluidized bed is formed in the gasification furnace 110 by introducing the gasifying agent into the high-temperature fluid medium introduced from the first cyclone separator 210.

  In addition, the gasification raw material containing organic solid raw materials such as coal such as lignite, petroleum coke (petro coke), biomass and tire chips is introduced into the fluidized bed in the introduction section 140a connected to the gasification furnace 110. The raw material input part 140c for performing is provided. The gasification raw material charged from the raw material charging unit 140c is guided to the gasification furnace 110 together with the fluidizing medium, and in the gasification furnace 110, the fluidizing medium fluidized by the gasifying agent has a temperature of about 700 ° C to 900 ° C. Gasification is caused by heat, and thereby gasification gas is generated. If the gasifying agent is water vapor and the gasification raw material is coal, a gasification gas mainly containing hydrogen, carbon monoxide, carbon dioxide, and methane is generated.

  The gasified gas generated in this way is sent to the second cyclone separator 130 through the delivery unit 110a together with the fluid medium. Although details will be described later, the ash generated by the combustion of the residue of the gasification raw material in the combustion furnace 120 is introduced into the gasification furnace 110 from the first cyclone separator 210 together with the fluidized medium. Ashes are also introduced into the cyclone separator 130 along with the gasification gas and the fluid medium.

  Further, the gasification furnace 110 communicates with the combustion furnace 120 via the discharge part 140b and the seal part 102b. This discharge part 140b is connected to the side wall facing the side wall to which the first cyclone separator 210 in the gasification furnace 110 is connected. Therefore, the fluid medium introduced from the first cyclone separator 210 flows in the gasification furnace 110 toward the discharge part 140b and is then discharged to the combustion furnace 120 through the seal part 102b. At this time, in the gasification furnace 110, a part of the input gasification raw material becomes unreacted, and the residue of the gasification raw material is discharged to the combustion furnace 120 together with the fluidized medium.

(Combustion furnace 120)
The combustion furnace 120 communicates with the gasification furnace 110 through the seal part 102b and the discharge part 140b, and the residue of the gasification raw material and the fluidized medium are introduced from the gasification furnace 110. The introduced residue of the gasification raw material and the fluidized medium are heated to about 1000 ° C. in the combustion furnace 120. Thereby, the residue of gasification raw material burns and becomes ash. Further, in the combustion furnace 120, in accordance with the introduction of the combustion gas from the lower side, a flow of the combustion exhaust gas is generated from the lower side to the upper side, and by this flow, the fluidized medium heated to about 1000 ° C. and the gasification raw material Ash generated from the residue is led out to the first cyclone separator 210 through the connecting portion 120a together with the combustion exhaust gas.

(First cyclone separator 210)
The first cyclone separator 210 includes a main body 210a, an introduction port 210b, a drop port 210c, and an exhaust port 210d. A mixture of a heated fluid medium (solid), ash (solid), and combustion exhaust gas (gas) introduced from the connection portion 120a is introduced into the main body 210a through the inlet 210b.

  The first cyclone separator 210 swirls the mixture (fluid medium (solid), ash (solid), combustion exhaust gas (gas)) introduced through the inlet 210b in the main body 210a, so that the first cyclone separator 210 has a predetermined particle size or more. The solid is dropped through the drop port 210c, and the scattered particles and gas which are solids having a particle diameter smaller than a predetermined particle size are exhausted through the exhaust port 210d positioned vertically above the drop port 210c.

  Specifically, the first cyclone separator 210 separates the fluid medium and a part of the ash into the drop port 210c, and the remaining ash (scattered particles) and combustion exhaust gas into the exhaust port 210d. As a result, the high-temperature fluid medium heated in the combustion furnace 120 and a part of the ash are again introduced into the gasification furnace 110 through the connecting pipe 212, and the above-described circulation is repeated thereafter.

  Here, the separation efficiency of the first cyclone separator 210 will be described. During rated operation, the fluid medium and a predetermined amount of ash to the dropping port 210c, and the remaining ash (scattered particles) and combustion exhaust gas to the exhaust port 210d. The separation efficiency of the first cyclone separator 210 (the amount of solid dropped from the dropping port 210c / the amount of solid contained in the introduced mixture) is designed.

In order to achieve the separation efficiency (hereinafter simply referred to as the first rated separation efficiency) in the first cyclone separator 210, for example, the particle size distribution of the solid in the introduced mixture as shown in FIG. The first cyclone separator 210 is designed with reference to FIG. More specifically, the desired separation efficiency (region shown by cross-hatching / (region shown by cross-hatching + region shown by cross-hatching in FIG. 2) is calculated with respect to the expected particle size distribution of the solid in the introduced mixture shown in FIG. If the area indicated by hatching)) is determined, the minimum particle size (separation minimum particle size, separation limit particle size) x _min of the solid that satisfies the determination is also determined.

…数式（１） Generally, in the cyclone separator, the separation minimum particle size x _min , the width B of the inlet of the cyclone separator, the flow rate u _i of the mixture (intake) at the inlet of the cyclone separator, and the cyclone separator are introduced. that solid and the density [rho _p of the density [rho _a gas to be introduced into the cyclone separator, a relationship shown in equation (1) below (dust collection technology and equipment, Japan powder industry Kyokai 1997, page 71). In Equation (1), C _c is a Cunningham correction coefficient (a coefficient for deriving a resistance force considering slip), and N is the number of turns of the mixture (intake) (converted as 5).

... Formula (1)

Therefore, when designing the first cyclone separator 210, the first cyclone separation is performed so that the flow rate of the introduced mixture at the rated operation becomes the separation minimum particle size x _min that satisfies the first rated separation efficiency. The flow rate of the mixture introduced into the vessel 210 is determined, and the shape of the first cyclone separator 210 (for example, the diameter of the introduction port) will be designed to achieve the flow rate of the mixture.

  On the other hand, the exhaust port 210d is connected to the ash dust collector (bag filter) 152 via the heat exchanger 150, and the scattered particles (remaining ash) and the combustion exhaust gas guided to the exhaust port 210d are converted into the heat exchanger 150. After being cooled, the ash dust collector 152 separates the particles into scattered particles and combustion exhaust gas. Here, the separated scattered particles are discarded, and the combustion exhaust gas is released to the atmosphere from a pipe or the like (not shown).

(Second cyclone separator 130)
The second cyclone separator 130 includes a main body 130a, an introduction port 130b, a drop port 130c, and an exhaust port 130d. A fluid medium (solid) and ash (solid) are introduced into the main body 130a together with the gasification gas (gas) generated in the gasification furnace 110 through the delivery part 110a and the introduction port 130b.

  The second cyclone separator 130 swirls the mixture (gasification gas (gas), fluid medium (solid), ash (solid)) introduced through the inlet 130b, so that a solid having a predetermined particle diameter or more is obtained. While being dropped through the drop port 130c, scattered particles and gas which are solids having a particle diameter smaller than a predetermined particle diameter are exhausted through an exhaust port 130d positioned vertically above the drop port 130c. More specifically, the second cyclone separator 130 separates the fluid medium and most of the ash into the drop port 130c, and the gasified gas and the remaining ash (scattered particles) into the exhaust port 130d. .

  The gasified gas and the scattered particles (ash) separated into the exhaust port 130d by the second cyclone separator 130 pass through the delivery pipe 160a to downstream equipment (reforming furnace 160, indirect heat exchanger 162, spray tower 164). To the mist separator 166). Here, if a large amount of ash is introduced into downstream equipment, there is a risk of affecting each equipment.

  Therefore, the second cyclone separator 130 is configured so that only ash that does not affect downstream equipment is separated into the exhaust port 130d, that is, most of the ash is separated into the drop port 130c. A separation efficiency (hereinafter simply referred to as a second rated separation efficiency) is designed.

When designing the second cyclone separator 130, similarly to the first cyclone separator 210 described above, the flow rate of the mixture to be introduced at the rated operation, that is, generated in the gasifier 110 at the rated operation. The flow rate of the mixture introduced into the second cyclone separator 130 is determined so that the amount of gasified gas becomes the separation minimum particle size x _min that satisfies the second rated separation efficiency, and the flow rate of the mixture is achieved. In addition, the shape of the second cyclone separator 130 (for example, the diameter of the inlet) is designed.

  The fluid medium and most of the ash separated by the second cyclone separator 130 are again introduced into the gasification furnace 110 through the drop port 130c and the drop tube 130e, and the gasified gas and the scattered particles are exhausted. It is sent to the reforming furnace 160 through the port 130d and the delivery pipe 160a.

(Reforming furnace 160, indirect heat exchanger 162, spray tower 164, mist separator 166)
The reforming furnace (oxidation reforming furnace) 160 adds oxygen or air to the gasification gas generated in the gasification furnace 110 and reforms the tar contained in the gasification gas at 900 ° C. to 1500 ° C. (oxidation reforming). ) Thus, most of the tar is removed by the reforming furnace 160. Further, the ash (scattered particles) contained in the gasification gas together with tar becomes molten slag by the heat of the reforming furnace 160. The indirect heat exchanger 162 performs heat exchange between the gasification gas introduced from the reforming furnace 160 and water vapor, collects the sensible heat of the gasification gas with water vapor, and sets the outlet temperature of the gasification gas to 300 ° C. Bring to 600 ° C.

  The spray tower 164 cools the gasification gas which became 300 degreeC-600 degreeC to about 70 degreeC by spray-spraying about 40 degreeC water on gasification gas. Thereby, tar and sludge remaining in the gasification gas are condensed and removed from the gasification gas. The mist separator 166 sprays water with water droplets smaller than the particle diameter in the spray tower 164, so that the spray tower 164 cannot sufficiently separate and remove the mist (mist-like) contained in the gasification gas. Tar and sludge) are condensed and removed.

  The gasified gas from which tar and sludge have been removed by the mist separator 166 is processed by a desulfurizer, a deammonizer, and a demineralizer (not shown). Specifically, sulfur and sulfur compounds are removed from the gasification gas in a desulfurizer, nitrogen compounds such as ammonia are removed in a deammonizer, and chlorine and chlorine compounds are removed in a demineralizer. The gasified gas thus generated in the gasification furnace 110 is purified gasified gas from which tar and ash are removed.

  By the way, when the required amount of purified gasification gas decreases, the amount of gasification raw material to be input to the gasification furnace 110 may be decreased, and the amount of gasification gas generation in the gasification gas generation system 100 may be decreased. is there. In this case, the flow rate of the mixture at the inlet 130b of the second cyclone separator 130 is reduced, and the separation efficiency of the second cyclone separator 130 is lower than the second rated separation efficiency. As a result, the amount of ash (scattered particles) exhausted from the exhaust port 130d increases from that during rated operation, and molten slag increases in the reforming furnace 160, or the indirect heat exchanger 162 and the mist separator 166 are blocked. There is a risk of doing so.

  Here, using the mechanical mechanism, the diameter of the inlet 130b in the second cyclone separator 130 is changed (the diameter is reduced), the flow rate of the mixture is increased, and the second cyclone separator 130 It is also conceivable to increase the separation efficiency. However, since the gasification gas introduced into the second cyclone separator 130 is as high as 700 ° C. to 900 ° C., it is difficult to use a mechanical mechanism for the second cyclone separator 130.

  Therefore, it is conceivable to reduce the separation efficiency of the first cyclone separator 210 below the first rated separation efficiency and reduce the ash introduced into the gasification furnace 110. In order to reduce the separation efficiency of the first cyclone separator 210, there is a method of reducing the flow rate of the mixture in the first cyclone separator 210. For example, it is conceivable to reduce the flow rate of the combustion gas for burning the residue of the gasification raw material or fuel supplied to the combustion furnace 120, but in this case, the fuel is not sufficiently burned and the fluid medium is desired. There is a possibility that the temperature cannot be heated to the temperature, or the fluid medium cannot be sufficiently led out to the connection part 120a.

  Further, it is conceivable to reduce the flow rate of the mixture by changing the diameter of the inlet 210b in the first cyclone separator 210 (increasing the diameter) using a mechanical mechanism. Since the combustion exhaust gas and fluidized medium introduced into the separator 210 are as high as about 1000 ° C., it is difficult to use a mechanical mechanism for the first cyclone separator 210.

  Therefore, in the present embodiment, even if the cyclone system 200 is used in a high temperature field, the separation efficiency of the cyclone separator is reliably controlled with a simple configuration.

(Cyclone system 200)
The cyclone system 200 includes a first cyclone separator 210, a connecting tube 212, a gas supply unit 214, and a scattered particle detection unit 216.

  The gas supply unit 214 includes a supply pipe 214a, a valve 214b, and a flow rate adjustment unit 214c, and supplies gas to the connection pipe 212 from a gas supply source (not shown). Here, the space on the seal portion 102a side in the connecting pipe 212 is sealed (sealed) with a fluid medium. Further, since the vicinity of the drop port 210c of the first cyclone separator 210 is negative pressure, the space on the drop port 210c side in the connecting pipe 212 is negative pressure. For this reason, the gas supplied from the gas supply unit 214 to the connecting pipe 212 does not flow out before the seal unit 102a, but flows back into the first cyclone separator 210 through the drop port 210c of the first cyclone separator 210. Will be.

  With such a simple configuration that the gas supply unit 214 supplies gas to the connecting pipe 212, the gas flows back into the first cyclone separator 210 through the drop port 210 c, and the flow rate of the mixture introduced into the first cyclone separator 210 Can be reduced. That is, the separation efficiency of the first cyclone separator 210 can be reduced.

  As described above, the gas supply unit 214 supplies gas to the connecting pipe 212 to reduce the separation efficiency of the first cyclone separator 210 and increase the amount of ash exhausted from the exhaust port 210d. The amount of ash falling from 210c can be reduced.

  That is, if the upper limit value of the separation efficiency in the first cyclone separator 210 is set to the first rated separation efficiency, the amount of gasification gas generated in the gasification furnace 110 is reduced and the separation efficiency of the second cyclone separator 130 is increased. Even if it decreases, the separation efficiency of the first cyclone separator 210 can be reduced by supplying the gas to the connecting pipe 212 by the gas supply unit 214, and the first cyclone separator 210 and the second cyclone separator 130 can be reduced. It becomes possible to maintain the balance of the separation efficiency.

  In other words, the upper limit value (first rated separation efficiency) of the separation efficiency of the solid having a predetermined particle diameter or more of the first cyclone separator 210 is the mixture introduced during the rated operation of the first cyclone separator 210. The lower limit value of the separation efficiency of the solids having a predetermined particle diameter or more of the first cyclone separator 210 is determined by the upper limit value of the gas supply amount to the connection pipe 212 by the gas supply unit 214. That's what it means.

  Since the ash exhausted from the exhaust port 210d of the first cyclone separator 210 is in the form of powder, it can be easily collected (collected) by the ash dust collector 152.

  Further, as described above, the space on the seal portion 102a side of the connecting pipe 212 is sealed (sealed) with a fluid medium, so that the gas supplied from the gas supply portion 214 is introduced into the gasification furnace 110 through the seal portion 102a. It will never be done. Therefore, the gas supplied by the gas supply unit 214 may be any gas (for example, air) regardless of the gasifying agent in the gasification furnace 110.

  FIG. 3 is an explanatory diagram for explaining an example of the gas supply unit 214. As shown in FIG. 3, in the present embodiment, the supply pipe 214 a of the gas supply unit 214 is a pipe inclined at least partly vertically downward from the valve 214 b toward the connecting pipe 212. With such a configuration, it is possible to avoid a situation in which the fluid medium and ash dropped through the dropping port 210c enter the supply pipe 214a.

  FIG. 4 is an explanatory diagram for describing a modified example of the gas supply unit 214. The supply pipe 214a only needs to be able to avoid a situation in which the fluid medium and ash dropped through the drop opening 210c enter the supply pipe 214a. For example, as shown in FIG. The pipe may be inclined vertically downward as it goes from the valve 214b to the connecting pipe 212 over the entire length. Further, as shown in FIG. 4B, the connection pipe 212 is provided on the inner surface of the connection pipe 212 and is positioned vertically above the opening connected to the connection pipe 212 in the supply pipe 214 a, and is connected to the connection pipe 212 from the inner surface of the connection pipe 212. You may provide the projection part 218 protruded and formed in the center side of the diameter.

  The flow rate adjusting unit 214c monitors the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the mist separator 166, the pressure loss value of the indirect heat exchanger 162 and the mist separator 166, and a scattered particle detection unit to be described later. Based on the signal transmitted from 216, the flow rate of the gas supplied to the connecting pipe 212 is adjusted by adjusting the opening of the valve 214b.

  More specifically, when the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the mist separator 166 exceeds a predetermined value, the flow rate adjusting unit 214c opens the valve 214b. Then, the flow rate adjusting unit 214c adjusts the flow rate of the gas supplied to the connecting pipe 212 by adjusting the opening of the valve 214b according to the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the mist separator 166. .

  The fact that the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the pressure loss value of the gasification gas in the mist separator 166 are higher than those during the rated operation indicates that the gasification sent from the second cyclone separator 130 is gasified. This means that the gas contains a lot of ash (scattered particles), that is, the separation efficiency in the second cyclone separator 130 has decreased. Therefore, the flow rate adjusting unit 214c controls the valve 214b when the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the mist separator 166 becomes equal to or higher than a predetermined value (a value higher than the pressure loss value during rated operation). Thus, the supply of gas to the connecting pipe 212 is started, and the separation efficiency of the first cyclone separator 210 is lowered. By doing so, in the first cyclone separator 210, the amount of scattered particles (ash) exhausted from the exhaust port 210d is increased, and the ash that is dropped from the drop port 210c and introduced into the gasification furnace 110 is decreased. be able to. Thereby, even if the separation efficiency in the second cyclone separator 130 is reduced, the absolute amount of ash introduced into the second cyclone separator 130 can be reduced, and the gas delivered from the second cyclone separator 130 can be reduced. It becomes possible to reduce the amount of scattered particles (ash) contained in the chemical gas.

  On the other hand, the flow rate adjusting unit 214c adjusts the opening degree of the valve 214b based on the signal transmitted from the scattered particle detecting unit 216 in order to maintain the amount of scattered particles (ash) exhausted from the exhaust port 210d at a predetermined amount. The flow rate of the gas supplied to the connecting pipe 212 is adjusted.

  The scattered particle detection unit 216 detects the concentration of the scattered particles (ash) exhausted from the exhaust port 210d, and transmits a signal indicating the detection result to the flow rate adjustment unit 214c.

  The flow rate adjusting unit 214c controls the valve 214b in accordance with the signal transmitted from the scattered particle detecting unit 216, and the amount of scattered particles (ash) exhausted from the exhaust port 210d and the falling from the dropping port 210c. It becomes possible to maintain the amount of ash to be maintained at a desired value.

  As described above, according to the gasified gas generation system 100 and the cyclone system 200 according to the present embodiment, only gas is supplied to the connecting pipe 212 connected to the drop port 210c of the first cyclone separator 210. With a simple configuration, it is possible to control the separation efficiency of the first cyclone separator 210 to which a fluid medium such as about 1000 ° C. introduced from the combustion furnace 120 is introduced, that is, used in a high temperature field.

(Cyclone control method)
Subsequently, a cyclone control method using the above-described cyclone system will be described. FIG. 5 is a flowchart for explaining the processing flow of the cyclone control method. Here, the detailed process of the separation efficiency control of the first cyclone separator 210 in the gasification gas generation system 100 will be described with reference to FIG.

  In the cyclone control method, processing is started by a periodic timer interruption at a predetermined time interval. When the timer interruption occurs, first, the flow rate adjusting unit 214c temporarily stores the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the mist separator 166 in a memory (not shown) (S300).

  Subsequently, the flow rate adjusting unit 214c adjusts the opening degree of the valve 214b through a predetermined function based on the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the pressure loss value of the gasification gas in the mist separator 166. Calculate (S302). Since such a function can be created using various existing methods, description thereof is omitted.

  For example, when the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the pressure loss value of the gasification gas in the mist separator 166 are less than a predetermined value, the flow rate adjustment unit 214c sets the opening degree of the valve 214b. It is calculated as 0 (that is, the gas supply unit 214 is closed). Further, when the pressure loss value of the gasification gas becomes a predetermined value or more, the opening degree of the valve 214b (a value exceeding 0) is determined according to the value.

  Then, the flow rate adjustment unit 214c adjusts the valve 214b to the calculated opening degree (S304). Then, gas is supplied from the gas supply source to the connection pipe 212 through the valve 214b and the supply pipe 214a, and the gas flows back into the first cyclone separator 210 from the connection pipe 212 through the drop port 210c.

  In this embodiment, the flow rate adjusting unit 214c is configured to open the valve 214b based on both the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the pressure loss value of the gasification gas in the mist separator 166. However, even if the opening degree of the valve 214b is adjusted based on either the pressure loss value of the gasification gas in the indirect heat exchanger 162 or the pressure loss value of the gasification gas in the mist separator 166, Good.

  As described above, also by the cyclone control method according to the present embodiment, when the pressure loss value of the gasification gas in the indirect heat exchanger 162 and the mist separator 166 exceeds a predetermined value, the flow rate adjustment unit 214c opens the valve 214b. Then, the gas supply unit 214 starts supplying gas to the connecting pipe 212. As a result, the gas is allowed to flow back into the first cyclone separator 210 through the drop port 210c, and the separation efficiency of the first cyclone separator 210 can be reduced.

  By doing so, in the first cyclone separator 210, the amount of scattered particles (ash) exhausted from the exhaust port 210d is increased, and the ash that is dropped from the drop port 210c and introduced into the gasification furnace 110 is decreased. be able to. Thereby, when the separation efficiency in the second cyclone separator 130 is lowered, the absolute amount of ash introduced into the second cyclone separator 130 can be reduced, and the gasification sent from the second cyclone separator 130 can be reduced. It becomes possible to reduce the amount of scattered particles (ash) contained in the gas.

(Example)
FIG. 6 shows the exhaust gas exhausted from the exhaust port 210d of the first cyclone separator 210 when no gas is supplied to the connecting pipe 212 (comparative example) and when gas is supplied to the connecting pipe 212 (example). It is a figure which shows the density | concentration of the scattering particle | grains in it. As shown in FIG. 6, when the gas is not supplied to the connecting pipe 212 (shown in black in FIG. 6), the concentration of scattered particles in the exhaust gas exhausted from the exhaust port 210d of the first cyclone separator 210 is adjusted. On the other hand, when the gas is supplied to the connecting pipe 212 (shown in white in FIG. 6), the concentration of scattered particles in the exhaust gas exhausted from the exhaust port 210d of the first cyclone separator 210 is about 7 times. Met.

  As can be seen from this result, the concentration of scattered particles in the exhaust gas exhausted from the exhaust port 210d of the first cyclone separator 210 can be reduced with a simple configuration in which the gas supply unit 214 only supplies gas to the connecting pipe 212. The concentration of ash that is raised, that is, dropped from the drop opening 210c, can be lowered. In other words, the separation efficiency of the first cyclone separator 210 can be reduced only by the gas supply unit 214 supplying gas to the connecting pipe 212.

  As mentioned above, although preferred embodiment of this invention was described referring an accompanying drawing, it cannot be overemphasized that this invention is not limited to this embodiment. It will be apparent to those skilled in the art that various changes and modifications can be made within the scope of the claims, and these are naturally within the technical scope of the present invention. Is done.

  For example, in the above-described embodiment, the cyclone system 200 is installed in the gasification gas generation system 100. However, the cyclone system 200 may be installed in another high temperature field such as a boiler, or in a low temperature field (normal temperature field). May be. For example, the cyclone system can be used for vacuum cleaner dust collection.

  Further, in the embodiment described above, the circulating fluidized bed type gasification furnace 110 that flows sand in the horizontal direction has been described as an example, but the moving bed is formed by the sand flowing down vertically by its own weight. A circulating moving bed type gasification furnace can also be used.

  Furthermore, in the embodiment described above, the gas supply unit 214 includes the flow rate adjustment unit 214c. However, the gas supply unit 214 may not include the flow rate adjustment unit 214c. For example, the user may perform indirect heat exchange. Depending on the pressure loss value of the gasification gas in the vessel 162 or the mist separator 166, the gas supply to the connecting pipe 212 may be started or stopped by opening and closing the valve 214b.

  In addition, the gas supply unit 214 is connected to the connecting pipe 212 according to the amount of the gasification raw material that is input to the raw material input unit 140c regardless of the pressure loss value of the gasification gas in the indirect heat exchanger 162 or the mist separator 166. The flow rate of the gas to be supplied may be determined.

  The present invention relates to a cyclone system, a gasification gas generation system, and a cyclone control method for controlling the separation efficiency of a cyclone separator.

DESCRIPTION OF SYMBOLS 100 ... Gasification gas production system 110 ... Gasification furnace 120 ... Combustion furnace 162 ... Indirect heat exchanger 166 ... Mist separator 200 ... Cyclone system 210 ... 1st cyclone separator (cyclone separator)
210a ... Main body 210b ... Inlet port 210c ... Drop port 210d ... Exhaust port 212 ... Connecting pipe 214 ... Gas supply part 214a ... Supply pipe 214b ... Valve 214c ... Flow rate adjustment part 216 ... Scattered particle detection part

Claims (8)

A mixture in which a solid and a gas are mixed is introduced through an introduction port, and the mixture is swirled to drop a solid having a predetermined particle size or more through the drop port, and is a scattering particle that is a solid having a particle size less than the predetermined particle size. And a cyclone separator that exhausts the gas through an exhaust port located vertically above the drop port;
A connecting pipe connected to the drop port;
Said via a supply pipe connected to the communication tube by supplying gas into the connecting pipe, the cyclone separator gas supplying section for backflow the gas inside through the chute,
Equipped with a,
The cyclone system according to claim 1, wherein the supply pipe is a pipe inclined vertically downward from one end toward the other end connected to the connecting pipe . A scattering particle detection unit that detects the concentration of the scattering particles exhausted from the exhaust port,
The gas supply unit includes a flow rate adjusting unit that adjusts a flow rate of a gas supplied to the connecting pipe,
2. The cyclone system according to claim 1, wherein the flow rate adjusting unit adjusts a flow rate of a gas supplied to the connecting pipe according to a detection result of the scattered particle detecting unit. The separation efficiency of the cyclone separator having a predetermined particle size or more is determined by the flow rate of the mixture at the inlet,
The diameter of the inlet is set so that the flow rate of the mixture at the inlet at the rated operation of the cyclone separator is the fastest,
The cyclone system according to claim 1 or 2, wherein the separation efficiency is lowered by supplying gas to the connecting pipe by the gas supply unit. A gasification furnace that fluidizes the fluidized medium and gasifies the input gasification raw material with the heat of the fluidized medium to generate a gasified gas;
A combustion furnace in which the fluidized medium discharged from the gasification furnace and the residue of the gasification raw material are guided, the fluidization medium is heated and the residue of the gasification raw material is burned to generate ash;
A mixture of the heated fluid medium, the ash, and the combustion exhaust gas discharged from the combustion furnace is introduced through an introduction port, and a solid having a predetermined particle diameter or more is dropped by swirling the mixture. A cyclone separator that drops through a mouth and exhausts scattered particles and gas that are solids less than a predetermined particle diameter through an exhaust port positioned vertically above the drop port;
A connecting pipe connected to the drop port;
Said via a supply pipe connected to the communication tube by supplying gas into the connecting pipe, the cyclone separator gas supplying section for backflow the gas inside through the chute,
Equipped with a,
The gasification gas generation system according to claim 1, wherein the supply pipe is a pipe inclined vertically downward from one end to the other end connected to the connecting pipe . An indirect heat exchanger that cools the gasification gas by performing heat exchange between the gasification gas generated in the gasification furnace and the heat medium;
A mist separator that further cools the gasified gas cooled by the indirect heat exchanger and removes mist from the gasified gas;
With
The said gas supply part supplies gas to the said connection pipe, when the pressure loss value of the gasification gas in at least one of the said indirect heat exchanger and the said mist separator is more than predetermined value. 5. The gasified gas generation system according to 4. The gas supply unit includes a flow rate adjusting unit that adjusts a flow rate of a gas supplied to the connecting pipe,
The flow rate adjusting unit adjusts the flow rate of gas supplied to the connecting pipe according to a pressure loss value of gasification gas in at least one of the indirect heat exchanger and the mist separator. 6. The gasified gas generation system according to 5.   A gasification furnace that fluidizes the fluidized medium and gasifies the input gasification raw material with the heat of the fluidized medium to generate a gasified gas;
  A combustion furnace in which the fluidized medium discharged from the gasification furnace and the residue of the gasification raw material are guided, the fluidization medium is heated and the residue of the gasification raw material is burned to generate ash;
  A mixture of the heated fluid medium, the ash, and the combustion exhaust gas discharged from the combustion furnace is introduced through an introduction port, and a solid having a predetermined particle diameter or more is dropped by swirling the mixture. A cyclone separator that drops through a mouth and exhausts scattered particles and gas that are solids less than a predetermined particle diameter through an exhaust port positioned vertically above the drop port;
  A connecting pipe connected to the drop port;
  A gas supply unit configured to supply a gas to the connecting pipe, thereby causing the gas to flow back into the cyclone separator through the dropping port;
  An indirect heat exchanger that cools the gasification gas by performing heat exchange between the gasification gas generated in the gasification furnace and the heat medium;
  A mist separator that further cools the gasified gas cooled by the indirect heat exchanger and removes mist from the gasified gas;
With
  The gas supply unit includes a flow rate adjusting unit that adjusts a flow rate of a gas supplied to the connecting pipe,
  The gas flow adjusting unit adjusts the flow rate of the gas supplied to the connecting pipe according to the pressure loss value of the gasified gas in at least one of the indirect heat exchanger and the mist separator. Gas generation system. A gasification furnace that fluidizes the fluidized medium and gasifies the input gasification raw material with the heat of the fluidized medium to generate gasified gas, the fluidized medium discharged from the gasification furnace, and the above A combustion furnace in which a residue of a gasification raw material is guided, heats the fluidized medium and burns the residue of the gasification raw material to generate ash, and the heated fluidized medium discharged from the combustion furnace, A mixture of ash and combustion exhaust gas is introduced through the inlet, and the mixture is swirled to cause a solid having a predetermined particle diameter or more to fall through the outlet and to be a solid having a particle diameter smaller than the predetermined particle diameter. A cyclone separator that exhausts particles and gas through an exhaust port positioned vertically above the dropping port, a connecting pipe connected to the dropping port, and supplying gas to the connecting pipe, Indirect heat that cools the gasified gas by exchanging heat between the gas supply unit that reversely flows the gas into the cyclone separator through the mouth and the gasified gas generated in the gasification furnace and the heat medium. A cyclone control method using an exchanger and a mist separator that further cools the gasified gas cooled by the indirect heat exchanger and removes mist from the gasified gas,
Determining whether the pressure loss value of the gasification gas in at least one of the indirect heat exchanger and the mist separator is a predetermined value or more;
When the pressure loss value is a predetermined value or more, supplying gas to the connecting pipe by the gas supply unit;
The cyclone control method characterized by including.

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