JP6708683B2 - Solid fuel gasification system - Google Patents

Description

The present invention relates to a gasification system for gasifying a solid fuel.

Coal is one of the important energy sources in the future because it has abundant reserves and is produced all over the world. Currently, anthracite and bituminous coal, which have a high calorific value per unit weight, are mainly used, but in the future, it is necessary to promote the use of subbituminous coal and brown coal, which account for about half of the reserves. Compared to bituminous coal and anthracite, subbituminous coal and lignite have a high water content and a low calorific value per unit weight on an anhydrous basis. In particular, lignite contains a very large amount of water of about 30 to 70 wt %, and dried lignite has a characteristic that it is easy to ignite spontaneously. For this reason, lignite is used only in the vicinity of the coal production area because it costs a lot to transport and store.

One of the measures to promote the use of lignite is a gasification system using lignite. This takes out the product gas mainly composed of CO and H ₂ from the brown coal, hydrogen the product gas, methane, methanol, dimethyl ether (DME; D i m ethyl E ther), and synthetic natural gas (SNG; S ynthetic N atural G as) and so on. As a result, brown coal is converted into high-value-added transportable product gas, which is used as electricity, chemical raw materials, fuel for social infrastructure, etc.

In the gasification furnace used in this gasification system, a spouted bed method is often used in which the temperature inside the furnace is increased to melt slag and the coal ash is separated from the produced gas. Since the molten slag flows down on the surface of the furnace wall made of a refractory material, the refractory material on the furnace wall may be melted by erosion of the molten slag. In order to continue the operation of the gasification furnace for a long time, it is essential to form molten slag on the surface of the furnace wall continuously to form a slag coating that suppresses melting loss of the refractory material.

It is known that brown coal has a large number of coal species having a low ash content (for example, several percent or less), and even if the same coal species is used, the ash melting point varies depending on changes in ash properties. In order to gasify brown coal, a method of operating a gasification furnace and a gasification system that maintain the formation of a slag coating in the furnace with a low ash coal type and a change in ash properties are required. Furthermore, in the gasification of lignite, a gasification furnace and a gasification system that can reduce the power of the lignite drying in the pretreatment are required.

For example, in Patent Document 1, an ash modifier (minerals such as limestone and silica, and oxide powder such as slag, refractory material and cement) is added to brown coal, and ash content is 2 to 19 wt% (desirably 6 to 10 wt%. %) to maintain the formation of the slag coating in the furnace.

Further, in Patent Document 2, slag powder recovered from the gasification furnace is added to a char supply system for recirculating the char generated in the gasification furnace to the gasification furnace, and the char is supplied into the furnace for slag coating in the furnace. A gasification system that maintains formation is described.

JP2012-172080A

JP, 2014-136764, A

One of the measures to reduce the power of brown coal drying is a gasification system in which the moisture content of the brown coal supplied to the gasifier is increased. In this gasification system, lignite with high moisture content needs to be crushed and transported to a gasification furnace.

However, in a gasification system that supplies a solid fuel with a high water content (high-moisture solid fuel) to a gasification furnace, the water contained in the solid fuel is present between the drying means and the gasification furnace, that is, in the pulverizer and the transportation system. May evaporate and condense in places where the temperature drops. When water condenses in the crusher or the transportation system, solid fuel adheres to the condensed water as a starting point and further solid fuel adheres and accumulates, reducing the supply amount of solid fuel or blocking the crusher or the transportation system. May lead to.

For example, in a crusher that is operated at a temperature higher than normal temperature (for example, about 40 to 70° C.), water tends to be condensed near the wall surface and the outlet that are lower than the operation temperature. Also, if solid fuel locally heated to a high temperature due to frictional heat from pulverization of solid fuel adheres and accumulates inside the crusher (for example, near the wall surface), the solid fuel may spontaneously ignite inside the crusher. There is. Further, in the hopper that stores the solid fuel in the transport system, when the outside air temperature is lower than the temperature inside the hopper, water tends to be condensed near the wall surface and the inlet/outlet of the solid fuel.

Patent Document 1 describes an operating method in which mineral powder such as limestone and silica sand and oxide powder such as slag, refractory material and cement are added to brown coal as an ash modifier. However, it does not mention the location where an ash regulator is added and the effect other than ash control. Since no reference is made to the attachment/deposition of solid fuel due to the condensation of water vaporized from the solid fuel inside the crusher or the transportation system, and the prevention of spontaneous combustion, the method of Patent Document 1 discloses the method of high moisture solid fuel ( Application of lignite etc.) is not assumed.

Patent Document 2 describes an operation method in which slag powder recovered from the gasification furnace is added to a hopper of a char supply system for recirculating the char generated in the gasification furnace to the gasification furnace. However, the method of Patent Document 2 does not assume application of high-moisture solid fuel.

As described above, the methods of Patent Document 1 and Patent Document 2 do not assume the application of high-moisture solid fuels, and therefore are a matter of concern when high-moisture solid fuels are applied, that is, the amount of moisture evaporated from the solid fuels. It does not consider prevention of self-ignition and blockage due to solid fuel adhesion/accumulation due to condensation. Therefore, the high-moisture solid fuel cannot be applied to the processes described in Patent Documents 1 and 2.

Therefore, the present invention provides a gasification system capable of performing stable operation even when a high-moisture solid fuel is applied, drying power is suppressed to a low level, and the high-moisture solid fuel is crushed and conveyed. To aim.

In order to achieve the above object, the gasification system according to the first to third aspects of the present invention includes a drying unit, a pulverizing unit, an air flow conveying unit, and a gasification furnace. The drying means dries the solid fuel and the crushing means crushes the solid fuel. The air flow carrying means carries the air flow of the solid fuel dried by the drying means and crushed by the crushing means to the gasification furnace. The gasification furnace gasifies the solid fuel carried by the airflow carrying means.

In gasification system according to a first aspect of the present invention includes an inorganic material, and a powder having a moisture absorption, at least箇why on the supplied powder supply system to the gasifier from the grinding means, flour And a controller that determines the amount of powder supplied from the powder supply system based on the predicted value of the amount of water vaporized at the body supply location .

A gasification system according to a second aspect of the present invention is a dedusting unit that separates and collects char from the produced gas generated in a gasification furnace, and a char that is collected by the dedusting unit is conveyed to a gasification furnace by air flow. And a char airflow transporting means. In the second aspect, a powder containing an inorganic substance and having a hygroscopic property is provided in at least one location from the crushing means to the gasification furnace and at least one location from the char air flow carrying means to the gasification furnace. A powder supply system for supplying the powder and a control device for determining the supply amount of the powder from the powder supply system based on the predicted value of the amount of water evaporated at the powder supply location are provided.

A gasification system according to a third aspect of the present invention includes a dedusting unit that separates and recovers char from the produced gas generated in the gasification furnace, and the char recovered by the dedusting unit is used as an air flow carrying unit. The solid fuel is supplied to the gasification furnace for air flow. Water In a third aspect, includes an inorganic material, and a powder having a moisture absorption, the at least one箇why on the supplied powder supply system to the gasifier from the grinding means and evaporated in the supply location of the powder And a controller that determines the amount of powder supplied from the powder supply system based on the predicted value of the amount .

When the solid fuel having a high water content (for example, 25 wt% or more) is crushed by the crushing means and is air-flow conveyed to the gasification furnace by the air-flow conveying means, the solid fuel is condensed by the water evaporated from the solid fuel in the crushing means or the air-flow conveying means. Fuel may adhere or accumulate.

In order to suppress such adhesion and volume of solid fuel, in the gasification system of the first to third aspects, a powder containing an inorganic substance and having hygroscopicity is provided between the pulverizing means and the gasification furnace. A powder supply system for supplying powder is provided. By supplying the powder, it is possible to dehumidify the water evaporated from the solid fuel, and to prevent the solid fuel from adhering and accumulating due to the condensation of the water.

In particular, the crushing means is operated at a temperature higher than normal temperature (for example, about 40 to 70° C.), and the frictional heat at the time of crushing locally raises the operating temperature of the crushing means, so that the solid fuel adhered/accumulated spontaneously ignites. There is a risk of Therefore, by configuring the powder supply system so as to supply the powder to the crushing means, it is possible to suppress the solid fuel from adhering to and depositing inside the crushing means, and to prevent the solid fuel from spontaneously igniting in the crushing means. Can be prevented.

Therefore, a high-moisture solid fuel is applied, the drying power in the drying means is suppressed to a low level, and a gasification system capable of stable operation is constructed even when the high-moisture solid fuel is crushed and conveyed. be able to.
In addition, since a control device that determines the supply amount of the powder from the powder supply system based on the predicted value of the amount of water vaporized at the powder supply location is provided, the supply amount of the powder can be reduced to the required minimum. Can be suppressed to.

Furthermore, in the second aspect, since the powder is supplied from the char airflow conveying means to the gasification furnace, the moisture evaporated from the char is dehumidified and the adhesion and deposition of the char due to the condensation of the moisture is suppressed. be able to.

A fourth aspect of the present invention is the gasification system according to any one of the first to third aspects, wherein the air flow carrying means has a hopper for fuel. The powder supply system individually supplies the powder to the crushing means and the fuel hopper.

A fifth aspect of the present invention is the gasification system according to the second aspect, wherein the air flow carrying means has a hopper for fuel, and the char air flow carrying means has a hopper for char. The powder supply system individually supplies the powder to the crushing means, the hopper for fuel, and the hopper for char.

A sixth aspect of the present invention is the gasification system according to the fourth or fifth aspect, wherein the drying means has first and second drying means. The crushing means crushes the solid fuel dried by the first drying means. The second drying means dries the solid fuel crushed by the crushing means. The airflow conveying means supplies the solid fuel pulverized by the pulverizing means to the upper burner of the gasification furnace, and the airstream conveying system for the upper burner, and the solid fuel pulverized by the pulverizing means supplies to the lower burner of the gasification furnace. An air flow carrier system for the lower burner is provided. The fuel hopper includes an upper burner hopper provided in the upper burner airflow transfer system and a lower burner hopper provided in the lower burner airflow transfer system. The powder supply system individually supplies the powder to the hopper for the upper burner and the hopper for the lower burner.

When the airflow conveying means is provided with a fuel hopper, when the outside air temperature is lower than the inside temperature of the hopper, water evaporated from the solid fuel may condense near the wall surface or near the inlet/outlet of the solid fuel.

In order to suppress the solid fuel from adhering to the fuel hopper and its volume, in the gasification system according to the fourth to sixth aspects, the powder is supplied to the fuel hopper. By supplying the powder, it is possible to suppress the generation of condensed water inside the hopper, and to prevent the supply amount of solid fuel from decreasing and the solid fuel conveying system from being blocked.

Furthermore, in the fifth aspect, since the powder is supplied to the hopper for char, it is possible to prevent blockage of the char transport system.

According to the gasification system of the present invention, stable operation can be performed even when high-moisture solid fuel is applied, drying power is suppressed to a low level, and high-moisture solid fuel is crushed and conveyed.

It is a systematic diagram which shows typically the high moisture coal gasification system which concerns on 1st Embodiment of this invention. It is a systematic diagram which shows typically the high moisture coal gasification system which concerns on 2nd Embodiment of this invention. It is a systematic diagram which shows typically the high moisture coal gasification system which concerns on 3rd Embodiment of this invention. It is a systematic diagram which shows typically the high moisture coal gasification system which concerns on 4th Embodiment of this invention. It is a functional block diagram of the control apparatus provided in the high moisture coal gasification system of FIG.

Hereinafter, a high moisture coal gasification system according to an embodiment of the present invention will be described with reference to the drawings.

(First embodiment)
FIG. 1 shows a system (powder) for supplying a powder containing an inorganic substance and having a hygroscopic property (hereinafter referred to as a hygroscopic powder containing an inorganic substance) between the pulverizing means of the solid fuel 1 and the gasification furnace. The system diagram of the high moisture coal gasification system provided with the body supply system is shown.

As shown in FIG. 1, the solid fuel 1 is dried by a drying device (drying means) 2, crushed by a crushing device (crushing means) 3, and then pressurized and stored at a predetermined pressure by a lock hopper 5 to be fed hopper. Transferred to 6. In the feed hopper 6, the solid fuel 1 is entrained in the inert gas 8 and supplied to the gasification furnace 19 via the solid fuel carrier pipe 12 and the solid fuel burner 13. The transport path of the solid fuel 1 from the lock hopper 5 to the gasification furnace 19 via the feed hopper 6 flows the solid fuel 1 dried by the drying device 2 and crushed by the crushing device 3 into the gasification furnace 19. An air flow carrying means for carrying is configured.

Here, N ₂ or CO ₂ is suitable for the inert gas 8 used to transfer and convey the solid fuel 1. When N ₂ is used as the inert gas 8, it is preferable to use nitrogen 17 produced by supplying the air 14 to the air separator 16. In contrast, when using CO ₂ in the inert gas 8, CO ₂ (hereinafter, recovered CO ₂ is referred to as (101)) was recovered in the gasification system preferably used. For example, a part of the recovered CO ₂ (101) is extracted, the pressure of the recycled CO ₂ compressor 59 is increased to a predetermined pressure, and the recovered CO ₂ (102) is used. The flow rate of the recycled CO ₂ (102) is adjusted by the recycled CO ₂ flow rate adjusting valve 58. In the present embodiment, a gasification system in which CO ₂ is used as the inert gas 8 will be described.

When the solid fuel 1 is transferred from the lock hopper 5 to the feed hopper 6, the lock hopper pressure equalizing valve 9 and the feed hopper pressure equalizing valve 10 are opened to equalize the pressure of the lock hopper 5 and the feed hopper 6 before opening the transfer valve 7. .. Further, by introducing an inert gas 8 (CO _{2 in} this embodiment) for transfer into the lock hopper 5, the transfer stagnation of the solid fuel 1 at the outlet of the lock hopper 5 and the transfer valve 7 is prevented. The pressure adjusting valve 11 is used for adjusting the pressure of each hopper during transfer.
From the pressure control valve 11, CO ₂ containing fine solid fuel 1 (dusty) is exhausted. This exhausted CO ₂ may be reused as the inert gas 8 or may be mixed with the system of the stored CO ₂ (103). When mixed with the system of stored CO ₂ (103), it is necessary to remove the dust in the CO ₂ exhausted by the dedusting process.

The solid fuel 1 transferred to the feed hopper 6 is entrained in an inert gas 8 (CO _{2 in} this embodiment), and is supplied to a gasification furnace 19 via a solid fuel carrier pipe 12 and a solid fuel burner 13. .. The solid fuel 1 charged into the gasification furnace 19 is mixed with oxygen 18 similarly charged from the solid fuel burner 13 to be gasified, and a high-temperature generated gas 20 is generated. The main components of the produced gas 20 are CO and H ₂ .

The oxygen 18 introduced into the gasification furnace 19 is produced by the air separator 16. The pressure of the air 14 is increased by the compressor 15 and supplied to the air separator 16 to separate it into nitrogen 17 and oxygen 18. Here, in order to reduce the power of the air separator 16, water may be electrolyzed with electric power generated by natural energy such as sunlight or wind power, and at least a part of oxygen 18 may be produced to improve energy efficiency. I do not care.

The generated gas 20 having a high temperature is supplied to the generated gas cooling unit 21. In the produced gas cooling unit 21, the spray water 62 whose pressure has been increased to a predetermined pressure is introduced to cool the produced gas 20. In order to atomize the spray water 62, a atomization nozzle is installed at the inlet of the spray water 62 of the produced gas cooling unit 21.

As the spray water 62, water 46 recovered from the product gas after the shift reaction described later, cooling water of molten slag generated in the gasification furnace 19 or the like is used to complete the system in which the amount of industrial water used is reduced. And good.

Further, the generated gas cooling unit 21 is supplied with the steam 60 containing the scattered fuel generated in the drying device 2 for the solid fuel 1, and the surplus water contained in the solid fuel 1 is also effectively used. In many cases, the drying device 2 is operated at a pressure close to normal pressure, and the generated gas cooling unit 21 is operated under pressure. Therefore, the steam 60 containing the scattered fuel is supplied to the produced gas cooling unit 21 after being pressurized by the compressor 61.

In the present embodiment, the system in which the steam 60 containing the scattered fuel is supplied to the upstream side of the spray water 62 and mixed with the high-temperature generated gas 20 is shown. If the temperature of the produced gas 20 after being mixed with the steam 60 containing the scattered fuel can be maintained at about 1000° C. or higher, an aqueous shift reaction (CO+H ₂ O→CO ₂₎ by the introduced steam and CO in the produced gas can be achieved. +H ₂ ) progresses. If the shift reaction can proceed in the produced gas cooling unit 21, this leads to a reduction in the amount of shift reaction catalyst used in the downstream shift reactor and a reduction in the amount of shift reaction water 39 used.

Here, when the high temperature generated gas 20 is cooled in a short time and the generated gas cooling unit 21 is downsized to reduce the construction cost of the gasification system, the spray water 62 is supplied from the upstream side of the steam 60 containing the scattered fuel. It is also possible to use a system (not shown) for supplying the.

The generated gas 22 after cooling has the char 24 entrained in the dust removing device (dust removing means) 23 removed, and halogen-based substances such as chlorine in the water washing tower 31 and fine particles that cannot be removed by the dust removing device 23. And the sulfur content is further removed by the desulfurizer 32.

The char 24 separated from the produced gas 22 after cooling is stored in the char lock hopper 25, appropriately transferred to the char feed hopper 26, and thereafter, transferred to the gasification furnace 19 via the char transport pipe 63 and the char burner 64. It is thrown in. The transfer path of the char 24 from the char lock hopper 25 to the gasification furnace 19 via the char feed hopper 26 constitutes a char airflow transfer means for transferring the char 24 collected by the dust removing device 23 to the gasification furnace 19. .. The inert gas 8 is used as the carrier gas for the char 24. In the present embodiment, a system using recycled CO ₂ (102) as the carrier gas as the carrier gas will be described.

The method of transferring and transporting the char 24 is the same as the method of the solid fuel 1 described above. When the char 24 is transferred, the char lock hopper pressure equalizing valve 28 and the char feed hopper pressure equalizing valve 29 are opened to equalize the pressure of the char lock hopper 25 and the char feed hopper 26, and then the char transfer valve 27 is opened to transfer the char 24. To do. An inert gas 8 (CO _{2 in the} present embodiment) is introduced for promoting the transfer of the char 24 and adjusting the pressure of the hopper, and the pressure of these hoppers is adjusted by adjusting the opening degree of the char system pressure adjusting valve 30.

On the other hand, the desulfurized product gas 33 containing CO, H ₂ , CO ₂ , and H ₂ O (steam) as main components is heated to about 200 to 300° C. by the product gas heat exchanger 34 and the product gas heater 35. It is heated and fed to the first shift reactor 36. Here, the heating temperature of the produced gas 33 after desulfurization is set according to the characteristics of the shift reaction catalyst filled in the shift reactor.

In the first shift reactor 36, the produced gas 33 after desulfurization is mixed with the steam 42 for shift reaction, and the shift reaction proceeds. If the shift reaction, which is an exothermic reaction, proceeds excessively, there is a danger that the reaction gas and the shift reaction catalyst may be damaged by the high-temperature product gas. For this reason, it is advisable to install a plurality of stages of shift reactors and to carry out the shift reaction stepwise while cooling the produced gas. In this embodiment, a case where two shift reactors are installed will be described.

In addition, the shift reaction rate is adjusted according to the use of the produced gas (H ₂ , methane, methanol, DME (dimethyl ether), SNG (synthetic natural gas), and the content of CO and H ₂ in the produced gas 38 after the shift reaction is adjusted. To adjust this shift reaction rate, it is advisable to adjust the shift reaction rate by operating conditions such as the temperature of the shift reactor and the amount of steam added, and by increasing or decreasing the catalyst filling amount. A system that bypasses the two-shift reactor 37 may be provided.

The produced gas 33 after desulfurization is supplied to the second shift reactor 37 after being cooled to a predetermined temperature downstream of the first shift reactor 36. For cooling, the heat exchanger 41 of the product gas after the first shift reaction and the water for the shift reaction may be used, and the heat of the shift reaction may be used for preheating the steam 42 for the shift reaction.

The product gas 38 after the shift reaction is at a temperature of about 40° C. in the heat exchanger 34 for the product gas, the heat exchanger 40 for the product gas after the shift reaction and the water for the shift reaction, and the cooler 44 for the product gas after the shift reaction. Is cooled down.

Condensed water generated in this cooling process is separated in the knockout drum 45 and is recovered as water 46 recovered from the product gas 38 after the shift reaction. Although not shown in FIG. 1, the water 46 recovered from the product gas 38 after the shift reaction is preferably reused in the gasification system as the spray water 62 or the like. The water 46 recovered from the product gas 38 after the shift reaction may contain by-products such as methanol generated from CO and H ₂ O (steam) remaining in the product gas 38 after the shift reaction. .. The water 46 recovered from the product gas 38 after the shift reaction is sprayed on the product gas cooling unit 21 and evaporated to decompose into by-products such as methanol. This eliminates the need for a treatment device for the by-product contained in the water 46 recovered from the product gas 38 after the shift reaction.

The product gas 38 after the shift reaction that has been cooled to about 40° C. has CO ₂ removed in the CO ₂ absorption tower 47 and becomes the product gas 48 after CO ₂ absorption. The generated gas 48 after the CO ₂ absorption is used as a fuel and a chemical raw material for power generation and social infrastructure.

In the CO ₂ absorption tower 47, the CO ₂ absorption liquid 53 containing methyldiethanolamine as a main component comes into contact with the generated gas 38 after the shift reaction, thereby separating and removing CO ₂ . CO ₂ absorbed CO ₂ absorbing liquid 49 is a heater 51 of the CO ₂ absorbing solution heat exchanger 50, CO ₂ absorbing solution is heated to 100 ° C. or higher is supplied to the CO ₂ regeneration tower 52. In the CO ₂ regeneration tower 52, CO ₂ contained in the CO ₂ absorbing liquid 49 that has absorbed CO ₂ is released.

Thus, the CO ₂ absorbing liquid 49 that CO ₂ absorption reuse becomes possible as the CO ₂ absorbing liquid 53. CO ₂ absorbing liquid 53 is pressurized by the pressurizing pump 54 of the CO ₂ absorbing solution is cooled to about 40 ° C. In the heat exchanger 50 of the CO ₂ absorbing solution is supplied to the CO ₂ absorber 47.

In the present embodiment, although the gasification system installed CO ₂ recovery system by chemical absorption with methyl diethanolamine, it may be used other CO ₂ recovery method.

In the gasification system as described above, when the solid fuel 1 having a high water content (for example, 25 wt% or more) is gasified, the water content of the solid fuel 1 at the outlet of the drying device 2 is the same as that of a conventional general system (about 15 wt%). Below) is set higher. Therefore, in the high-moisture coal gasification system of the present embodiment, an energy-efficient high-moisture coal gasification system in which the power for drying the solid fuel 1 by the drying device 2 is reduced as compared with the conventional general system. Can build

In this system, the solid fuel 1 having high water content is supplied to the crushing device 3, and the solid fuel 1 may adhere to the inner wall of the crushing device 3 or the like. The crushing device 3 is operated at a temperature higher than normal temperature (for example, about 40 to 70° C.), and there is a possibility that the crushing device 3 locally reaches a higher temperature due to frictional heat during crushing. Therefore, inside the crushing device 3, water remaining in the solid fuel 1 may evaporate. The evaporated water may be cooled by the outside air in the vicinity of the inner wall of the crushing device 3 and condensed, and may adhere to and accumulate on the inner wall together with the solid fuel 1. The solid fuel 1 adhered and deposited inside the crushing device 3 may impede the operation of the crushing device 3 or cause spontaneous combustion.

Therefore, the grinder 3 is provided with a supply system for the hygroscopic powder 4A containing an inorganic substance. The powder 4</b>A supplied into the crushing device 3 absorbs the water evaporated in the crushing device 3, is discharged together with the solid fuel 1, and is stored in the lock hopper 5.

In the lock hopper 5, the inert gas 8 is supplied to raise the pressure to a predetermined pressure, and the solid fuel 1 is stored for up to several tens of minutes at maximum (the storage time varies depending on the hopper capacity and the supply amount of the solid fuel 1). If, for example, the solid fuel 1 having a temperature higher than the outside temperature is stored, the inert gas 8 having a temperature higher than the outside temperature is supplied at the time of pressurization or transfer, or the outside temperature decreases during the storage, The internal temperature of the lock hopper 5 becomes higher than the external temperature.

In this case, water evaporated from the solid fuel 1 may condense on the wall surface of the lock hopper 5 where the ambient temperature decreases due to heat radiation to the outside air or in the vicinity of the entrance/exit. In the system for conveying the solid fuel 1 to the gasification furnace 19 by air flow, if the solid fuel 1 adheres and accumulates together with condensed water, the entrance and exit of the hopper may be blocked.

Therefore, the lock hopper 5 is provided with a supply system for the hygroscopic powder 4B containing an inorganic substance. The powder 4B supplied into the lock hopper 5 absorbs moisture evaporated from the solid fuel 1 stored in the lock hopper 5, and is transferred to the feed hopper 6 through the solid fuel transfer valve 7 together with the solid fuel 1. To be done.

Since the solid fuel 1 transferred to the feed hopper 6 is stored in the feed hopper 6 as in the case of the lock hopper 5 described above, water evaporated from the solid fuel 1 may be condensed. When the solid fuel 1 adheres and accumulates with the condensed water at the inlet of the hopper, the inner wall, the vicinity of the inlet of the transfer pipe 12, the inside of the transfer pipe 12, etc., the flow rate of the solid fuel 1 supplied to the gasification furnace 19 is significantly increased. May decrease.

Here, it is conceivable that the water generated in the feed hopper 6 may not be absorbed only by the powder 4B supplied from the lock hopper 5 and transferred from the lock hopper 5 together with the solid fuel 1. In this case, although not shown, if a supply system of hygroscopic powder containing an inorganic substance is further installed in, for example, the feed hopper 6 or the solid fuel carrier pipe 12 between the feed hopper 6 and the gasification furnace 19. good.

Further, in this system, the char 24 having a high water content is collected and stored in the char lock hopper 25, transferred to the char feed hopper 26, and then the char transport pipe 63 and It is charged into the gasification furnace 19 via the char burner 64. If, for example, the char 24 having a temperature higher than the outside temperature is stored, the inert gas 8 having a temperature higher than the outside temperature is supplied at the time of pressurization or transfer, or the outside temperature decreases during the storage, The inside temperature of the charlock hopper 25 becomes higher than the outside temperature.

In this case, the water evaporated from the char 24 may condense on the wall surface of the charlock hopper 25 or the vicinity of the entrance/exit where the ambient temperature decreases due to heat radiation to the outside air. If the char 24 adheres/accumulates together with the condensed water, the entrance/exit of the hopper may be blocked.

Therefore, a supply system for the hygroscopic powder 4C containing an inorganic substance is installed in the charlock hopper 25. The powder 4C supplied into the charlock hopper 25 absorbs moisture evaporated from the char 24 stored in the charlock hopper 25, and is transferred to the char feed hopper 26 through the char transfer valve 27 together with the char 24. It

Finally, the hygroscopic powder containing an inorganic substance will be described. Examples of hygroscopic powders containing inorganic substances include coal ash, waste incineration ash, zeolite (including artificial zeolite made from coal ash, etc.), silica gel, calcium carbonate and the like.

For example, when the high-moisture coal gasification system of the present embodiment is installed in the vicinity of a brown coal boiler operating near a differential coal boiler or a brown coal mine, coal ash generated in these boilers has a hygroscopic property containing an inorganic substance. It should be effectively used as powder. When the high-moisture coal gasification system of this embodiment is introduced adjacent to a waste incinerator, waste incinerator ash generated in this waste incinerator may be used.

Organic matter (unburned content) contained in these coal ash and waste incineration ash is gasified in the gasification furnace 19, and the inorganic matter is finally melted into slag in the gasification furnace 19. The molten slag can suppress the elution of heavy metals into the inundation, which is a concern with coal ash and waste incineration ash, and can be effectively used as a roadbed material or aggregate. As a result, it can contribute to the detoxification of ash generated in boilers and waste incinerators and the expansion of recycling.

By gasifying the high-moisture solid fuel 1 with the above system, a gasification system with excellent energy efficiency can be constructed by reducing the drying power of the solid fuel 1.

In the present embodiment, the crushing device 3, the lock hopper 5, and the charlock hopper 25 are provided with the powder supply systems for supplying the hygroscopic powders 4A, 4B, and 4C containing the inorganic substances, respectively. A powder supply system for supplying powder to any one or two of 3, the lock hopper 5, and the charlock hopper 25 may be used. In addition to these, a powder for supplying hygroscopic powder containing an inorganic substance may be used. It may be a body supply system.

(Second embodiment)
FIG. 2 shows a system diagram of a high-moisture coal gasification system provided with a system for supplying the char 24 collected by the dust removing means to the air-fuel conveying means for solid fuel. In the present embodiment, parts different from those of FIG. 1 shown in the first embodiment will be mainly described. In the present embodiment, the plurality of solid fuel burners 13 and 13A are provided, and the char burner 64 is not provided.

As shown in FIG. 2, the char 24 collected by the dust removing device 23 is supplied to the lock hopper 5 and transferred to the feed hopper 6 together with the solid fuel 1. Here, the solid fuel 1 supplied from the pulverizer 3 at normal pressure and the char 24 supplied at a pressure substantially equal to the operating pressure of the gasification furnace 19 are supplied to the same lock hopper 5, and the feed hopper 6 is supplied. The operation procedure for transferring to the above will be described.

First, the solid fuel 1 crushed by the crusher 3 is supplied to the lock hopper 5 at about room temperature and pressure. The hygroscopic powder 4B containing an inorganic substance is supplied to the lock hopper 5 together with the solid fuel 1 during this period in which the lock hopper 5 is operated under normal pressure. When the solid fuel 1 in the lock hopper 5 has accumulated more than a predetermined amount, the solid fuel supply valve 65 is closed and the inert gas 8 is introduced to raise the pressure of the lock hopper 5 to the same pressure as the dust removing device 23.

Next, the char supply valve 66 is opened, and the char 24 accumulated in the dust removing device 23 is supplied to the lock hopper 5. Here, in order to smoothly supply the char 24, measures may be taken such as introducing the inert gas 8 into the pipe connecting the dust removing device 23 and the lock hopper 5 or installing a pressure equalizing pipe.

Here, since the dust remover 23 is operated at a temperature higher than the dew point of the generated gas 22 after cooling (for example, 230° C. or higher for 2.5 MPa), the char 24 is set to the operating temperature of the dust remover 23. It flows into the lock hopper 5 at a close temperature, that is, a temperature considerably higher than room temperature. Therefore, in the lock hopper 5, the high-temperature char 24 and the high-moisture solid fuel 1 come into direct contact with each other, and the sensible heat of the char 24 evaporates the water contained in the solid fuel 1. In order to prevent the condensation of water, the lock hopper 5 is supplied with hygroscopic powder 4B containing an inorganic substance to dehumidify. Further, although not shown, the recycled CO ₂ (102) that has been adiabatically compressed by the recycled CO ₂ compressor 59 and heated to a temperature higher than normal temperature is used as the inert gas 8, and the lock hopper 5 and the solid fuel burner 13 and A system that keeps the temperature up to 13 A and promotes evaporation of water contained in the solid fuel 1 may be used. While this system requires measures for heat retention (for example, installation of steam pipes and heaters for heat retention, heat insulation materials, etc.), it reduces the risk of evaporation moisture condensation due to temperature decrease, so hygroscopic powder containing inorganic substances The supply amount of the body 4B can be reduced. Further, since the solid fuel 1 and the inert gas 8 can be preheated and charged into the gasification furnace 19, the temperature in the gasification furnace 19 can be prevented from lowering.

Further, the char supply valve 66 is closed, the inert gas 8 is introduced, the pressure of the lock hopper 5 is increased, and the pressure is set to the same as that of the feed hopper 6.

Finally, the lock hopper equalizing valve 9 is opened, the feed hopper equalizing valve 10 is opened, and the pressure adjusting valve 11 equalizes the pressure of the solid fuel 1 with the feed hopper 6 continuously supplying the gasifier 19 with a constant pressure. The solid fuel transfer valve 7 is opened to transfer the solid fuel 1 and the char 24 from the lock hopper 5 to the feed hopper 6. In order to prevent the powder transfer from being stagnant at the bottom of the lock hopper 5, it may be vibrated by hitting, or the inert gas 8 may be introduced.

The solid fuel 1 and the char 24 transferred to the feed hopper 6 are carried by the inert gas 8 as an air stream, and are supplied to the gasification furnace 19 via the solid fuel carrying pipe 12 and the solid fuel burners 13 and 13A.

Here, as a method of transporting the solid fuel 1 and the char 24 from one feed hopper 6 to the plurality of solid fuel burners 13 and 13A, a distributor 67 is installed between the feed hopper 6 and the gasification furnace 19. There are a system in which the solid fuel carrier pipe 12 is branched and a system in which a plurality of solid fuel carrier pipes 12 from the feed hopper 6 are installed. In the present embodiment, the former will be described as an example, but either of them may be used, or both may be combined.

Further, in the present embodiment, the hygroscopic powders 4A and 4B containing the inorganic substance have been described as the system that supplies the crushing device 3 and the lock hopper 5, but the feed hopper 6, the solid fuel carrier pipe 12, and the distributor 67. For example, it may be supplied from another place from the crushing means to the gasification furnace.

As described above, the char 24 having a temperature higher than room temperature, which is collected by the dust removing device 23, is supplied to the carrier system of the solid fuel 1 supplied with high moisture, and is brought into direct contact with the solid fuel 1 at room temperature. It is conveyed to the gasification furnace 19 together with 1. Even when water contained in the solid fuel 1 is evaporated by the sensible heat of the char 24 during the transfer and transportation of the solid fuel 1, the moisture absorption including the inorganic substances input from the pulverizer 3 to the gasification furnace 19 as in the present embodiment. Dehumidify with water-soluble powder 4A, 4B to prevent condensation of water. As a result, it is possible to construct a gasification system for high-moisture solid fuel, which is excellent in energy efficiency by reducing the drying power of the solid fuel 1 and has a simple system that does not require the transport system for the char 24.

(Third Embodiment)
FIG. 3 shows a system in which solid fuel and char are conveyed by air flow to a gasification furnace by a plurality of systems, and powders containing an inorganic substance and having hygroscopicity are individually supplied to the crusher and each hopper of each system (powder). The system diagram of the high moisture coal gasification system provided with the body supply system is shown. In the present embodiment, parts different from those of FIG. 1 shown in the first embodiment will be mainly described.

The solid fuel 1 is dried by the drying device (first drying means) 2A and crushed by the crushing device 3, and then the lock hopper 5 for supplying the solid fuel 1 to the upper burner 68 and the solid fuel 1 are further added. It is supplied to a drying device (second drying means) 2B for drying. Here, the water content of the solid fuel 1 that has been dried by the drying device 2A is selected as a value that satisfies all of the crushing device 3, the air flow conveyance to the gasification furnace 19 and the temperature ensuring in the gasification furnace 19. A hygroscopic powder 4A containing an inorganic material is supplied to the crushing device 3 to dehumidify the moisture evaporated inside, thereby preventing moisture condensation inside.

The solid fuel 1 stored in the lock hopper 5 is transferred to the feed hopper 6, is entrained in the inert gas 8, and is introduced into the gasification furnace 19 via the solid fuel transfer pipe 69 to the upper burner and the upper burner 68. To be done. Hygroscopic powders 4B and 4F containing an inorganic substance are supplied to the lock hopper 5 and the feed hopper 6 to dehumidify the moisture evaporated inside the hopper and prevent moisture condensation inside.

Here, a plurality of stages of burners having different heights are installed in the gasification furnace 19, the lower part of the furnace is heated to a high temperature and the inorganic matter in the solid fuel 1 is melted into slag, and the upper part of the furnace is set to a temperature lower than that of the lower part of the furnace. A method of promoting gasification of combustible components (carbon, hydrogen, etc.) in the solid fuel 1 is used. The use of CO ₂ as the inert gas 8 promotes the CO ₂ gasification reaction (C+CO ₂ →2CO), and the water content in the solid fuel 1 is increased to increase the steam gasification reaction (C+H ₂ O→CO). +H ₂ ). Therefore, the water content of the solid fuel 1 input from the upper burner 68 is set higher than the water content of the solid fuel 1 input from the lower burner 70. In the transport system for the solid fuel 1 to the upper burner 68, the solid fuel 1 having a higher water content is handled, and therefore the operation for preventing the water condensation is indispensable.

It is known that the water contained in the solid fuel 1 is roughly classified into two types: attached water attached to the particle surface and bound water chemically bound to the solid content by hydrogen bonding or ionic reaction. The former drying of the adhered water requires sensible heat up to the boiling point (100° C. under normal pressure) and latent heat of vaporization. On the other hand, the latter bound water requires, in addition to the above-mentioned sensible heat and latent heat, additional thermal energy for breaking the chemical bond to take out H ₂ O. From the viewpoint of improving the energy efficiency of the gasification system, it is desirable that the moisture content of the solid fuel 1 that has been dried by the drying device 2A is set to a value that will dry at least a portion of the adhered water.

Next, the solid fuel 1 input from the lower burner 70 is supplied to the drying device 2B and further dried. Thereafter, the solid fuel 1 is stored in the lower burner system lock hopper 72, transferred to the lower burner system feed hopper 73, and accompanied by the inert gas 8 to carry the lower burner system solid fuel carrier pipe 71 and the lower burner. It is charged into the gasification furnace 19 via 70. The lower burner lock hopper 72 and the lower burner feed hopper 73 are supplied with hygroscopic powders 4D and 4G containing an inorganic substance to dehumidify the water evaporated inside the hopper and prevent water condensation inside. .. Further, the char-feed hopper 26 is also supplied with the hygroscopic powder 4H containing an inorganic substance to dehumidify the water evaporated inside the hopper to prevent the water from condensing inside.

As described above, in the gasification system having a system for carrying the air stream of the solid fuel 1 and the char 24 in the gasification furnace 19 by a plurality of systems, the pulverizer 3, the solid fuel 1 and the hoppers 5, 72 of the carrier means are each provided with an inorganic substance. In order to prevent moisture from condensing, a separate powder supply system that contains hygroscopicity is separately provided to dehumidify. Further, by adjusting the water content suitable for gasification of the solid fuel 1, it is possible to construct a gasification system of high water content solid fuel having excellent energy efficiency by reducing drying power of the solid fuel which is a pretreatment.

(Fourth Embodiment)
FIG. 4 shows the water content of the dried solid fuel and the supply amount of the hygroscopic powder containing an inorganic substance, which is introduced into each of the pulverizing means, the solid-fuel and air-stream conveying means for char, and the gasification furnace. The high-moisture coal gasification system provided with the control device which adjusts each is shown. In this embodiment, parts different from those of FIG. 3 shown in the third embodiment will be mainly described.

As shown in FIG. 4, in the present embodiment, a system for supplying the hygroscopic powder 4E containing an inorganic substance to the gasification furnace 19 is newly provided. This is because the inorganic substance (ash) contained in the solid fuel 1 is added with the inorganic substance contained in the hygroscopic powder 4E containing the inorganic substance to change the flow rate of the inorganic substance to be melted and slagged in the gasification furnace 19 and the viscosity of the molten slag. This is because the function of adjusting and maintaining the slag coating formed in the lower portion of the gasification furnace 19 is added.

In the gasification system of the present embodiment, the pulverizing device 3, the lock hopper 5, the charlock hopper 25, the lower burner system lock that supplies the hygroscopic powder 4A, 4B, 4C, 4D, 4E containing the inorganic substance. A control device 78 incorporating the respective flow rate adjusting functions of the hopper 72 and the gasification furnace 19 is provided. The outline of the flow rate adjustment logic in the control device 78 will be described.

As shown in FIG. 5, first, from the analysis value of the solid fuel 1, the total water content (the water content contained in the solid fuel before drying) and the attached water content (bonded water content=total water content-bonded water content is calculated). , Ash content (that is, inorganic substances), ash melting point and ash composition, and industrial analysis (composition of organic substances such as C, H, and O). Thereby, the temperature inside the furnace for converting the ash into molten slag in the lower part of the gasification furnace 19, the flow rate of the solid fuel 1 to be charged into the gasification furnace 19, and the flow rate of the ash (inorganic matter) to be melted and slagified in the furnace are controlled. Set to 78.

Next, the water content of the solid fuel 1 to be charged into the gasification furnace 19 and the oxygen content for gasifying the solid fuel 1 are set. As a result, the target moisture (target moisture content) of the solid fuel after drying in the drying device 2A and the drying device 2B, the predicted value of the amount of water evaporated in the pulverizing device 3 together with the operating temperature of the pulverizing device 3, and the value after cooling The temperature of the generated gas 22 and the content ratio of water vapor are set. In the present embodiment, the predicted value of the amount of water evaporated in the crushing device 3, the temperature of the produced gas 22 after cooling, and the content ratio of steam are set in the control device 78, respectively.

Further, the supply temperature of the inert gas 8 and the target temperature of the inner wall of the char lock hopper 25 are set, and together with the analysis value of the solid fuel 1 described above, the lock hopper 5 and the lower burner for supplying the solid fuel 1 to the upper burner 68. The predicted values of the amount of water evaporated in the lock hopper 72 and the char lock hopper 25 of the system are predicted, and the predicted values are set in the control device 78.

The control device 78 prevents condensation of evaporated water inside the crushing device 3, the lock hopper 5, the lower burner system lock hopper 72, and the charlock hopper 25 based on these predicted values and the operating temperature of each device. The flow rates of the hygroscopic powders 4A, 4B, 4C, and 4D containing the inorganic substance, which are necessary for cleaning, are obtained.

Finally, from the viewpoint of maintaining the slag coating formed in the lower part of the gasification furnace 19 by adjusting the flow rate of the inorganic substance to be melted slag in the gasification furnace 19 and the viscosity of the molten slag, from the above 4A to 4D. When the total flow rate of the hygroscopic powder containing the inorganic substance to be fed into the gasification furnace 19 is insufficient, the gasification furnace 19 is arranged so that the hygroscopic powder 4E containing the lacking inorganic substance is fed into the gasification furnace 19. The flow rate of the powder 4E to be charged into the powder 4A, 4B is controlled by controlling a control valve or the like provided in the powder supply system so that the powder 4A, 4B, 4C, 4D having the calculated flow rate is supplied respectively. Supply 4C, 4D.

Although not shown in the present embodiment, a control logic for supplying the hygroscopic powder 4F containing an inorganic substance to the feed hopper 6 for the shortage of the hygroscopic powder 4B containing an inorganic substance supplied to the lock hopper 5. Alternatively, the control device 78 may be incorporated. The supply amount of the hygroscopic powders 4G, 4H containing an inorganic substance, which are supplied to the lower burner type feed hopper 73 and the char feed hopper 26, may be incorporated in the control device 78 as a logic to be set in the same manner as above.

As described above, based on the analysis value of the solid fuel 1, the target moisture of the dried solid fuel 1 is set, and the moisture absorption containing the inorganic substance for pulverizing the solid fuel 1 of this target moisture and establishing the air flow conveyance. By providing the control device 78 having a function of setting the supply amount of the volatile powder and further maintaining the slag coating logic formed in the gasification furnace 19, the drying power of the solid fuel 1 is reduced and energy efficiency is improved. A high-moisture solid fuel gasification system capable of stably transporting an excellent and high-moisture solid fuel 1 to a gasification furnace 19 is constructed.

The present invention is not limited to the above-described embodiments and modifications described as examples, and is not limited to the above-described embodiments and the like as long as the technical idea of the present invention is not deviated. Various modifications are possible according to the design, etc.

For example, as the high-moisture solid fuel 1 to be applied, other than brown coal (for example, low-grade coal such as subbituminous coal, biomass, waste, etc.) may be applied.

It is useful as a gasification system to which the high moisture solid fuel of the present invention is applied.

DESCRIPTION OF SYMBOLS 1... Solid fuel, 2, 2A, 2B... Drying device, 3... Crushing device, 4A, 4B, 4C, 4D, 4E, 4F, 4G, 4H... Hygroscopic powder containing an inorganic substance, 5... Lock hopper, 6 ... Feed hopper, 7... Solid fuel transfer valve, 8... Inert gas, 9... Lock hopper pressure equalizing valve, 10... Feed hopper pressure equalizing valve, 11... Pressure adjusting valve, 12... Solid fuel conveying pipe, 13, 13A... Solid fuel burner, 14... Air, 15... Compressor, 16... Air separator, 17... Nitrogen, 18... Oxygen, 19... Gasifier, 20... Product gas, 21... Product gas cooling section, 22... Generation after cooling Gas, 23... Dust remover, 24... Char, 25... Char lock hopper, 26... Char feed hopper, 27... Char transfer valve, 28... Char lock hopper pressure equalizing valve, 29... Char feed hopper pressure equalizing valve, 30... Char system Pressure regulating valve, 31... Water washing tower, 32... Desulfurization device, 33... Desulfurized product gas, 34... Product gas heat exchanger, 35... Product gas heater, 36... First shift reactor, 37... Two shift reactors, 38... Product gas after shift reaction, 39... Water for shift reaction, 40... Heat exchanger for product gas after shift reaction and water for shift reaction, 41... Production after first shift reaction Heat exchanger for gas and water for shift reaction, 42... Steam for shift reaction, 43... Heater for steam for shift reaction, 44... Cooler for product gas after shift reaction, 45... Knockout drum, 46... Shift reaction Water recovered from the later produced gas, 47... CO ₂ absorption tower, 48... CO ₂ absorbed produced gas, 49... CO ₂ absorbed CO ₂ absorbing liquid, 50... CO ₂ absorbing liquid heat exchanger, 51 ... CO ₂ absorption liquid heater, 52 ... CO ₂ regeneration tower, 53 ... CO ₂ absorption liquid, 54 ... CO ₂ absorption liquid pressurizing pump, 55 ... CO ₂ absorption liquid for regeneration heating, 56 ... CO ₂ absorption liquid Regeneration heater, 57... Steam for regenerating and heating CO ₂ absorbing liquid, 58... Reuse CO ₂ flow rate adjusting valve, 59... Reuse CO ₂ compressor, 60... Water vapor containing scattered fuel, 61... Compressor, 62 ... Spray water, 63... Char transport pipe, 64... Char burner, 65... Solid fuel supply valve, 66... Char supply valve, 67... Distributor, 68... Upper burner, 69... Solid fuel transport to upper burner Tube, 70... Lower burner, 71... Lower burner system solid fuel carrier pipe, 72... Lower burner system lock hopper, 73... Lower burner system feed hopper, 74... Lower burner system solid fuel transfer valve, 75 ...Lower burner type lock hopper Equalizing valve, 76 ... lower burner system feeds the hopper pressure equalizing valve, 77 ... lower burner system pressure control valve, 78 ... controller, 101 ... recovered _CO 2, 102 ... recycled _CO 2, 103 ... storage CO ₂

Claims (6)

A drying means for drying the solid fuel; a crushing means for crushing the solid fuel; an air flow carrying means for carrying the air flow of the solid fuel dried by the drying means and crushed by the crushing means to a gasification furnace; In the gasification system including the gasification furnace for gasifying the solid fuel that has been conveyed by the airflow conveying means,
Include inorganic and a powder having a moisture absorption, at least箇why on the supplied powder supply system to said gasification furnace provided from said comminution means,
Based on the predicted value of the amount of water that evaporates at the powder supply location, the powder from the powder supply system
A solid fuel gasification system, characterized in that a control device for determining the amount of body supply is provided . A drying means for drying the solid fuel; a crushing means for crushing the solid fuel; an air flow carrying means for carrying the air flow of the solid fuel dried by the drying means and crushed by the crushing means to a gasification furnace; The gasification furnace for gasifying the solid fuel carried by the airflow carrying means, the dedusting means for separating and collecting the char from the produced gas produced in the gasification furnace, and the dedusting means for collecting the char In a gasification system provided with a char airflow conveying means for conveying char to the gasification furnace by airflow,
A powder containing an inorganic substance and having a hygroscopic property is respectively supplied to at least one location from the crushing means to the gasification furnace and at least one location from the char airflow transport means to the gasification furnace. the powder supply system that is provided,
Based on the predicted value of the amount of water that evaporates at the powder supply location, the powder from the powder supply system
A solid fuel gasification system, characterized in that a control device for determining the amount of body supply is provided . A drying means for drying the solid fuel; a crushing means for crushing the solid fuel; an air flow carrying means for carrying the air flow of the solid fuel dried by the drying means and crushed by the crushing means to a gasification furnace; The gasification furnace for gasifying the solid fuel carried by the airflow carrying means, and the dedusting means for separating and recovering the char from the produced gas produced in the gasification furnace are provided. In the gasification system in which the recovered char is supplied to the air flow transfer means and is air flow transferred to the gasification furnace together with the solid fuel,
Include inorganic and a powder having a moisture absorption, at least箇why on the supplied powder supply system to said gasification furnace provided from said comminution means,
Based on the predicted value of the amount of water that evaporates at the powder supply location, the powder from the powder supply system
A solid fuel gasification system, characterized in that a control device for determining the amount of body supply is provided . The gasification system according to any one of claims 1 to 3, wherein:
The air flow carrying means has a hopper for fuel,
The solid fuel gasification system, wherein the powder supply system supplies the powder individually to each of the crushing means and the hopper for fuel. The gasification system according to claim 2, wherein
The air flow carrying means has a hopper for fuel,
The char airflow carrying means has a hopper for char,
The solid fuel gasification system, wherein the powder supply system supplies the powder individually to each of the crushing means, the fuel hopper, and the char hopper. A gasification system according to claim 4 or claim 5,
The drying means has first and second drying means,
The crushing means crushes the solid fuel dried by the first drying means,
The second drying means dries the solid fuel crushed by the crushing means,
The airflow conveying means includes an upper stream burner airflow conveying system for supplying the solid fuel pulverized by the pulverizing means to the upper burner of the gasification furnace, and the solid fuel pulverized by the pulverizing means of the gasification furnace. An air flow carrier system for the lower burner that supplies the lower burner is provided,
The fuel hopper includes an upper burner hopper provided in the upper burner airflow transfer system and a lower burner hopper provided in the lower burner airflow transfer system,
The solid fuel gasification system, wherein the powder supply system supplies the powder individually to each of the hopper for the upper burner and the hopper for the lower burner.

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