JP7286504B2 - Gasification facility and gasification combined cycle facility equipped with the same - Google Patents

Description

TECHNICAL FIELD The present invention relates to a gasification facility and an integrated gasification combined cycle facility having the same.

IGCC (Integrated Coal Gasification Combined Cycle) is a plant that supplies carbon-containing solid fuel such as coal into a gasification furnace, partially combusts the carbon-containing solid fuel, and gasifies it to generate combined power. known (for example, Patent Document 1).

In Patent Document 1, heat exchangers (superheater, evaporator, economizer, etc.) supported by hanger pipes (hanging pipes) in the gasification furnace, and steam drums connected to these heat exchangers A gasifier is described which is provided with a Here, the suspension pipes that support the heat exchanger are constructed so that water flows inside, thereby suppressing abnormal overheating of the suspension pipes. In this gasification furnace, the feed water heated by the suspension pipe is supplied to the economizer.

Further, Patent Document 2 describes a configuration in which a water pipe connected to the upper end of a cooling pipe that functions as a hanger for a heat exchanger in a gasification furnace is connected to a steam drum of the gasification furnace. ing. At this time, a water supply pipe is connected to the lower end of the cooling pipe. This water supply pipe is also connected to the water supply port of the heat exchanger (economy device) in the gasification furnace.

JP 2017-95530 A JP 2014-80506 A

In such suspension pipes, the temperature of the flowing water is generally controlled by setting the degree of subcooling at the outlet of the suspension pipe. Similarly, at the outlet of the economizer to which the water heated by the suspension pipe is supplied, the temperature of the circulating water may be controlled by setting the subcooling degree. This is to avoid steaming of water flowing through the suspension pipes and economizers. If steaming occurs, the heat transport medium changes state from water to steam, resulting in a significant decrease in the amount of heat transport. In this case, the metal temperature of the suspension pipe and the economizer may be excessively increased by the high-temperature generated gas, resulting in damage to the suspension pipe and the economizer.

At this time, as in Patent Document 1, in a configuration in which the water heated by the suspension pipe is supplied to the economizer, in other words, in a configuration in which the water supply system of the suspension pipe and the economizer are the same, There is a possibility that the water supply temperature to the economizer will be restricted due to the effect of the set subcooling degree. In this case, the temperature difference between the temperature of the product gas generated in the gasification furnace and the temperature of the feed water to the economizer becomes large, and the amount of steam generated in the heat exchanger provided in the gasification furnace becomes small. It may lead to a decrease in efficiency.

Further, for example, when the heat transfer surface of the economizer is relatively clean and the temperature of the feed water to the economizer is low, the product gas may be cooled more than necessary. This is not preferable because the temperature of the produced gas after heat exchange may fall below the temperature required for purification (for example, the activation temperature of the catalyst).

Further, as in Patent Document 2, when water is supplied from the same water supply pipe to the cooling pipe (suspension pipe) and the economizer in the gasification furnace, it is assumed that the subcooling degree is set for each of the water supply pipe and the economizer. If so, the subcooling degree set for the suspension pipe may impose a constraint on the feed water temperature to the economizer.

The present invention has been made in view of such circumstances, and provides a gasification facility that can efficiently utilize the heat of the generated gas generated in the gasification furnace and a combined gasification combined cycle facility equipped with the same. intended to provide

In order to solve the above problems, the gasification equipment according to the present invention and the integrated gasification combined cycle equipment having the same employ the following means.
That is, the gasification facility according to one aspect of the present invention has a plurality of product gas heat exchangers and a first drum for separating steam from a gas and a liquid, and the product gas produced from the carbon-containing solid fuel is used as the first feed water. a gasification furnace having a product gas heat exchange unit that heats to generate steam; a boiler for heating a third feedwater to produce steam, wherein the second feedwater is extracted from the third feedwater brought to a predetermined temperature, and the first feedwater is heated above the predetermined temperature by the boiler. is taken from the third feedwater heated to .

According to the gasification facility according to this aspect, the first feed water is heated by the product gas produced from the carbon-containing solid fuel, which has a plurality of product gas heat exchangers and the first drum for separating the steam from the gas and liquid. a gasification furnace having a product gas heat exchange section for generating steam through a gasifier, a suspension pipe supporting a plurality of product gas heat exchangers and through which a second feed water flows; and a third feed water. a boiler that heats to generate steam, the second feedwater is taken from the third feedwater that has been brought to a predetermined temperature, and the first feedwater is taken from the third feedwater that has been heated to a temperature higher than the predetermined temperature by the boiler. is
As a result, the first water supply and the second water supply can be taken out from the third water supply system having different temperatures, and the second water supply heated by the suspension pipe and flowing out is directly used as the first water supply in the product gas heat exchange section. It can be a configuration that does not lead to Therefore, even if the degree of subcooling is set for the second water supply flowing out of the suspension pipe, the temperature of the first water supply is not limited by the degree of subcooling. That is, in order to make the temperature of the first feed water optimal for the product gas heat exchange section, it is possible to make it higher than, for example, the temperature of the second feed water flowing out from the suspension pipe. This is realized, for example, by taking out as the first water supply a mixture of the high-temperature third water supply and the heated second water supply, or by taking out the high-temperature third water supply as the first water supply. In addition, the "optimal temperature" referred to here is, for example, a temperature that is heated so as to be as close as possible to a temperature that satisfies the subcooling degree set in the product gas heat exchanger (for example, 300 ° C. or higher and 330 ° C. below). By doing so, the temperature difference between the temperature of the product gas generated by the gasification furnace and the temperature of the first feed water can be reduced, so that the amount of steam generated in the product gas heat exchange section can be increased. That is, the heat (sensible heat) of the generated gas can be efficiently used. Moreover, since it is possible to suppress the generated gas from being cooled more than necessary, it is possible to avoid a phenomenon in which the temperature of the generated gas after heat exchange falls below the temperature required for refining.
The boiler may be an exhaust heat recovery boiler that utilizes the exhaust heat of the gas turbine, or may be an auxiliary boiler.

Further, in the gasification facility according to an aspect of the present invention, one of the plurality of product gas heat exchangers is an economizer that heats water, and the first feed water is supplied to the economizer.

According to the gasification facility according to this aspect, one product gas heat exchanger among the plurality of product gas heat exchangers is an economizer that heats water, and the first feed water is supplied to the economizer. ing.
This makes it possible to supply the economizer with the first feed water having a temperature that is as close as possible to the feed water temperature that satisfies the subcooling degree set in the economizer. At this time, if an evaporator connected to the economizer is provided as another product gas heat exchanger, steam can be efficiently generated.

Further, in the gasification facility according to one aspect of the present invention, one of the plurality of product gas heat exchangers is an evaporator that evaporates water, and the first drum is an evaporator that evaporates water. The first water supply is supplied to the first drum after gas-liquid separation is performed on the steam generated by the evaporator.

According to the gasification facility according to this aspect, one of the plurality of product gas heat exchangers is an evaporator that evaporates water, and the first drum is the evaporator. The steam is separated into gas and liquid, and the first feed water is supplied to the first drum.
As a result, the first feed water can be directly supplied to the first drum, so the temperature of the first feed water can be made higher than, for example, when the first feed water is supplied to the economizer. . Also, steam can be efficiently generated by the first evaporator.

Further, in the gasification facility according to one aspect of the present invention, the boiler has one combustion gas heat exchanger and another combustion gas heat exchanger, and the third feed water is the one combustion gas heat exchanger. and the other combustion gas heat exchanger, and the one combustion gas heat exchanger is installed downstream of the other combustion gas heat exchanger in the flow direction of the combustion gas, The first feedwater is taken from the third feedwater flowing through a first pipe connected to the outlet of the other combustion gas heat exchanger, and the second feedwater is taken from the outlet of the one combustion gas heat exchanger. It is taken out from the third feedwater flowing through a second pipe connecting the inlet of the other combustion gas heat exchanger.

According to the gasification facility according to this aspect, the boiler has one combustion gas heat exchanger and another combustion gas heat exchanger, and the third feed water is provided with one combustion gas heat exchanger and another combustion gas heat exchanger. The gas heat exchangers are led in order, and one combustion gas heat exchanger is installed downstream of the other combustion gas heat exchangers in the flow direction of the combustion gas, and the first feed water supplies heat to the other combustion gas. It is taken from a third feed water flowing through a first pipe connected to the outlet of the exchanger, and the second feed water connects the outlet of one combustion gas heat exchanger and the inlet of another combustion gas heat exchanger. It is taken out from the third water supply that flows through the second pipe that is present.
As a result, another combustion gas heat exchanger can be installed on the upstream side of the exhaust gas where the temperature of the exhaust gas is high. At this time, the first feed water is taken out from the third feed water flowing through the first pipe connected to the outlet of the other combustion gas heat exchanger, and the second feed water is connected to the outlet of the other combustion gas heat exchanger. It is taken out from the 3rd water supply which distribute|circulates the 2nd piping which carried out. Therefore, the first water supply temperature can be made higher than the second water supply temperature.

Further, in the gasification facility according to one aspect of the present invention, the first water supply is taken out from the first water intake part of the first pipe, and the second water supply flowing out from the suspension pipe is The water is returned to the first water return section provided in the first pipe on the upstream side of the first water intake section in the flow direction of the third water supply.

According to the gasification facility according to this aspect, the first water supply is taken out from the first water intake part of the first pipe, and the second water supply flowing out from the suspension pipe is the flow direction of the third water supply in the first pipe. , the water is returned to the first water return section provided in the first pipe on the upstream side of the first water intake section.
Thereby, the total flow rate of the flow rate of the third water supply flowing through the first pipe and the flow rate of the second water supply returned from the suspension pipe can be secured as the flow rate that can be supplied to the first water supply.

Further, in the gasification facility according to one aspect of the present invention, the first water supply is taken out from the first water intake part of the first pipe, and the second water supply flowing out from the suspension pipe is The third water supply is returned to the first water return section on the downstream side of the first water intake section in the flow direction of the third water supply.

According to the gasification facility according to this aspect, the first water supply is taken out from the first water intake part of the first pipe, and the second water supply flowing out from the suspension pipe is the flow direction of the third water supply in the first pipe. is returned to the first water return section on the downstream side of the first water intake section.
As a result, it is possible to prevent the temperature of the first water supply from dropping due to the second water supply returned from the suspension pipe.

Further, in the gasification facility according to one aspect of the present invention, a first flow control valve is provided in the first pipe downstream of the first water intake section in the flow direction of the third feed water in the first pipe. The first water return section is provided downstream of the first flow rate control valve in the flow direction of the third water supply in the first pipe.

According to the gasification facility according to this aspect, the first pipe downstream of the first water intake section in the flow direction of the third water supply in the first pipe is provided with the first flow rate adjustment valve, and the first return water is provided. The part is provided downstream of the first flow control valve in the flow direction of the third water supply in the first pipe.
Thereby, the flow rate of the second water supply flowing through the suspension pipe can be ensured.

Further, in the gasification facility according to one aspect of the present invention, a first water return pipe is provided between the outlet of the suspension pipe and the first water return section, and the first water return pipe is provided with a second water return pipe. A flow control valve is provided.

According to the gasification facility according to this aspect, the first water return pipe is provided between the outlet of the suspension pipe and the first water return section, and the first water return pipe is provided with the second flow rate adjustment valve. ing.
Thereby, the flow rate in the first water return pipe can be adjusted. As a result, the flow rate of the second water supply flowing through the suspension pipe can be adjusted. The degree of opening of the second flow control valve is determined by the controller based on, for example, a signal from a flowmeter provided in the first return pipe.

Further, in the gasification facility according to an aspect of the present invention, a branch pipe is provided in the first water return pipe on the upstream side of the second flow control valve in the flow direction of the second water supply in the first water return pipe. A third flow control valve is provided in the branch pipe.

According to the gasification facility according to this aspect, a branch pipe is connected to the first water return pipe on the upstream side of the second flow control valve in the flow direction of the second water supply in the first water return pipe, and the branch pipe , and a third flow control valve.
Thereby, the flow rate of the second water supply flowing through the suspension pipe can be adjusted by the third flow rate adjustment valve in addition to the second flow rate adjustment valve.
For example, the third flow control valve is used in the following cases. That is, when the flow rate of the second water supply is insufficient despite the opening degree of the second flow control valve being fully opened, the flow rate of the second water supply is increased by increasing the opening degree of the third flow control valve. ensure When the flow rate of the second water supply can be adjusted only by adjusting the opening degree of the second flow rate regulating valve, the opening degree of the third flow rate regulating valve is kept constant (for example, fully closed). Also, the degree of opening of the third flow control valve is determined by the controller based on, for example, a signal from a flowmeter provided in the first return pipe.
Further, when the flow rate of the second feed water is large with respect to the amount of steam generated by the boiler or the generated gas heat exchange section, the excess second feed water can be discharged out of the system through the branch piping.

Further, the gasification facility according to one aspect of the present invention includes a water pump that sends the second water supply to the suspension pipe, the second water supply is taken out from the second water intake part of the second pipe, and the The second water supply that has flowed out of the suspension pipe is supplied to the second water return part provided in the second pipe on the upstream side of the second water intake part in the flow direction of the third water supply in the second pipe. has been returned.

According to the gasification facility according to this aspect, the water supply pump that sends the second water supply to the suspension pipe is provided, and the second water supply is taken out from the second water intake part of the second pipe and flowed out from the suspension pipe. The water supply is returned to the second water return section provided in the second pipe on the upstream side of the second water intake section in the flow direction of the third water supply in the second pipe.
As a result, the second water supply circulates through the system composed of the second pipe and the suspension pipe, and the flow rate is adjusted by the water pump. Therefore, for example, even when the integrated gasification combined cycle facility is not in rated operation, that is, even when the amount of steam generated by the heat recovery boiler or the generated gas heat exchange unit is less than during rated operation, a constant amount of second feed water can be circulated in the suspension pipe.

Moreover, in the gasification facility according to one aspect of the present invention, the second water supply that has flowed out from the suspension pipe is fed to the first drum.

According to the gasification facility according to this aspect, the second water supply that has flowed out of the suspension pipe is sent to the first drum.
As a result, the second water supply heated by the suspension pipe and flowing out can be led to the first drum as a water supply system separate from the first water supply. Therefore, even if the degree of subcooling is set for the second water supply flowing out of the suspension pipe, the temperature of the first water supply is not limited by the degree of subcooling.

Further, in the gasification facility according to one aspect of the present invention, the boiler is an exhaust heat recovery boiler that heats the third feed water with exhaust gas from a gas turbine to generate steam.

According to the gasification facility according to this aspect, the boiler is an exhaust heat recovery boiler that heats the third feed water with the exhaust gas from the gas turbine to generate steam.

Further, an integrated gasification combined cycle facility according to one aspect of the present invention includes the gasification facility described above.

The integrated gasification combined cycle system according to this aspect includes the gasification system described above.
As a result, it is possible to provide an integrated gasification combined cycle system that can efficiently utilize the heat of the product gas generated in the gasification furnace.

ADVANTAGE OF THE INVENTION According to the gasification equipment which concerns on this invention, and gasification integrated cycle equipment provided with the same, the heat of the product gas produced|generated in the gasification furnace can be utilized efficiently.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic configuration diagram of an integrated gasification combined cycle system including gasification equipment according to each embodiment of the present invention; 1 is a schematic configuration diagram of a gasification facility according to a first embodiment of the present invention; FIG. FIG. 2 is a schematic configuration diagram of a gasification facility according to a second embodiment of the present invention; FIG. 4 is a diagram showing a configuration around a first water return unit shown in FIG. 2 or FIG. 3; It is the figure which showed the modification of the structure around a 1st water return part. FIG. 10 is a diagram showing another modified example of the configuration around the first water return section; FIG. 10 is a schematic configuration diagram of a gasification facility according to a third embodiment of the present invention; FIG. 5 is a schematic configuration diagram of a gasification facility according to a fourth embodiment of the present invention; FIG. 5 is a schematic configuration diagram of a gasification facility according to a fifth embodiment of the present invention;

[First embodiment]
A gasification facility according to a first embodiment of the present invention and an integrated gasification combined cycle facility having the same will be described below with reference to the drawings.
[Overall configuration of coal gasification combined cycle facility]
FIG. 1 shows a schematic configuration of a combined coal gasification combined cycle facility according to this embodiment.
An Integrated Coal Gasification Combined Cycle (IGCC) 1 includes a gasifier facility 3 . The gasification furnace equipment 3 uses air as an oxidant, and employs an air combustion system that generates combustible gas (produced gas) from a carbon-containing solid fuel such as coal. The integrated coal gasification combined cycle facility 1 refines the generated gas generated in the gasification furnace facility 3 in the gas refining facility 5 to obtain fuel gas, and then supplies the fuel gas to the gas turbine device 7 to generate power. That is, the integrated coal gasification combined cycle facility 1 is an air-combustion type (air-blown) power generation facility.
In addition, although air blowing is described in the present embodiment, oxygen blowing may be used. Coal, for example, is used as the carbon-containing solid fuel supplied to the gasifier facility 3 .

The integrated coal gasification combined cycle facility 1 includes a coal feeding facility 9, a gasification furnace facility 3, a char recovery facility 11, a gas refining facility 5, a gas turbine device 7, a steam turbine device 18, and a generator 19. , and a heat recovery steam generator (HRSG) 20 as a boiler.

The coal supply facility 9 is supplied with coal, which is a carbon-containing solid fuel, as raw coal from a coal supply bunker, and pulverizes the coal with a coal mill to produce pulverized coal pulverized into fine particles. Pulverized coal produced in the coal mill is pressurized by nitrogen gas as inert gas for transportation supplied from the air separation equipment 42 through the coal feed line 15 from each of the pulverized coal hoppers 14, and is sent to the gasification furnace equipment 3. supplied to An inert gas is an inert gas having an oxygen content of about 5% by volume or less, and typical examples thereof include nitrogen gas, carbon dioxide gas, and argon gas, but the content is not necessarily limited to about 5% or less.

The gasifier equipment 3 is supplied with the pulverized coal produced by the coal feed equipment 9, and the char (unreacted coal and ash) recovered by the char recovery equipment 11 is returned and supplied in a reusable manner. It is

A compressed air supply line 41 from the gas turbine device 7 (compressor 61) is connected to the gasification furnace equipment 3, and part of the compressed air compressed by the gas turbine device 7 is supplied to a booster 68 to a predetermined pressure. and can be supplied to the gasification furnace (gasification section) 16. The air separation equipment 42 separates and produces nitrogen and oxygen from atmospheric air, and the air separation equipment 42 and the gasification furnace equipment 3 are connected by a first nitrogen supply line 43 . A coal supply line 15 from a coal supply facility 9 is connected to the first nitrogen supply line 43 . A second nitrogen supply line 45 branching from the first nitrogen supply line 43 is also connected to the gasification furnace equipment 3, and a char return line 46 from the char recovery equipment 11 is connected to the second nitrogen supply line 45. It is connected. Furthermore, the air separation plant 42 is connected to the compressed air supply line 41 by an oxygen supply line 47 . The nitrogen separated by the air separation equipment 42 flows through the first nitrogen supply line 43 and the second nitrogen supply line 45 and is used as a carrier gas for coal and char. Further, the oxygen separated by the air separation equipment 42 is used as an oxidant in the gasification furnace equipment 3 by flowing through the oxygen supply line 47 and the compressed air supply line 41 .

The gasification furnace facility 3 includes, for example, a two-stage entrained bed type gasification furnace 16 . The gasification furnace equipment 3 partially burns the coal (pulverized coal) and char supplied therein with an oxidizing agent (air, oxygen) to gasify them into a generated gas. The inside of the gasification furnace 16 is pressurized, for example, 3 to 4 MPa (gauge pressure).
The burners 30 and 31 are provided in two stages, upper and lower. A combustor section 32 is provided at a position corresponding to the lower burner 30, and supplies heat for gasification by burning part of the pulverized coal. A reductor section 33 is provided at a position corresponding to the upper burner 31 to gasify pulverized coal.
A syngas cooler (produced gas heat exchange section) 35 is provided downstream of the reductor section 33 , and supplies the produced gas to the char recovery facility 11 after cooling it to a predetermined temperature. Steam is generated in the syngas cooler 35 and the generated steam is led to a heat recovery steam generator (HRSG) 20 . Details of the configurations of the syngas cooler 35 and the heat recovery boiler 20 will be described later.

A generated gas line 49 for supplying a generated gas to the char recovery equipment 11 is connected to the gasification furnace equipment 3 so that the generated gas containing char can be discharged.

The char recovery facility 11 includes a dust collection facility 51 and a supply hopper 52 . In this case, the dust collector 51 is composed of one or more cyclones or porous filters, and can separate the char contained in the product gas produced by the gasification furnace equipment 3 . The produced gas from which the char has been separated is sent to the gas purification facility 5 through the gas discharge line 53 . The supply hopper 52 stores the char separated from the generated gas by the dust collector 51 . A charbin 54 is arranged between the dust collector 51 and the supply hopper 52 . A plurality of feed hoppers 52 are connected to the charbin 54 . A char return line 46 from the supply hopper 52 is connected to the second nitrogen supply line 45 .

The gas refining equipment 5 performs gas refining by removing impurities such as sulfur compounds and nitrogen compounds from the generated gas from which the char is separated by the char recovery equipment 11 .
The gas refining equipment 5 refines the generated gas to produce fuel gas, which is supplied to the gas turbine device 7 . Since the generated gas from which the char has been separated still contains sulfur (such as H ₂ S), the gas refining equipment 5 removes and recovers the sulfur using an amine absorbent or the like for effective utilization.

Specifically, after passing through a COS converter 21, a scrubber 22, and a cooling scrubber 23, it is guided to an _H2S absorber 24 where _H2S is absorbed. The absorbent that has absorbed H ₂ S in the H ₂ S absorption tower 24 is regenerated in the absorbent regeneration tower 25 and returned to the H ₂ S absorption tower 24 . The H ₂ S gas separated from the absorbent in the H ₂ S absorption tower 24 is incinerated in the off-gas combustion furnace 26 and then guided to the flue gas desulfurization device 27 .

The gas turbine device 7 includes a compressor 61 , a combustor 62 and a gas turbine 63 , and the compressor 61 and gas turbine 63 are connected by a rotating shaft 64 . A compressed air supply line 65 from the compressor 61 and a fuel gas supply line 66 from the gas refining facility 5 are connected to the combustor 62 .

A combustion gas supply line 67 is connected between the combustor 62 and the gas turbine 63 . The gas turbine device 7 is provided with a compressed air supply line 41 extending from the compressor 61 to the gasification furnace equipment 3, and is provided with a booster 68 in the middle. Therefore, in the combustor 62, a portion of the compressed air supplied from the compressor 61 and at least a portion of the fuel gas supplied from the gas refining equipment 5 are mixed and burned to generate combustion gas. The resulting combustion gas is supplied toward the gas turbine 63 . The gas turbine 63 rotates the generator 19 by rotating the rotary shaft 64 with the supplied combustion gas.

The steam turbine device 18 comprises a steam turbine 69 connected to the rotating shaft 64 of the gas turbine device 7 . A condenser 72 is connected downstream of the steam turbine 69 . The generator 19 is connected to the proximal end of the rotating shaft 64 . Note that the generator 19 may be arranged between the steam turbine 69 and the gas turbine 63 . The exhaust heat recovery boiler 20 is connected to an exhaust gas line 70 from a gas turbine 63, and feed water led from a condenser 72 and combustion gas exhausted from the gas turbine 63 (hereinafter also referred to as "exhaust gas"). Steam is generated by exchanging heat with A steam supply line 71 is provided between the heat recovery boiler 20 and the steam turbine device 18 . The steam heated or superheated by the heat recovery boiler 20 includes steam generated by exchanging heat with the generated gas in the syngas cooler (SGC) 35 of the gasification furnace 16 . Therefore, in the steam turbine device 18 , the steam turbine 69 is rotationally driven by the steam supplied from the heat recovery boiler 20 , and the rotating shaft 64 is rotated to rotationally drive the power generator 19 .

A chimney 75 is connected to the outlet of the heat recovery steam generator 20, and combustion gas is released to the atmosphere. A gas cleaning facility may be provided at the outlet of the heat recovery boiler 20 .

[Operation of coal gasification combined cycle equipment]
Next, the operation of the integrated coal gasification combined cycle system 1 of this embodiment will be described.
In the coal gasification combined cycle facility 1 of the present embodiment, when raw coal (coal) is supplied to the coal feeding facility 9, the coal is pulverized into fine particles in the coal feeding facility 9 to become pulverized coal. . The pulverized coal produced in the coal supply facility 9 is supplied to the gasification furnace facility 3 through the first nitrogen supply line 43 with nitrogen supplied from the air separation facility 42 . Further, the char recovered by the char recovering equipment 11 described later is supplied to the gasification furnace equipment 3 through the second nitrogen supply line 45 with nitrogen supplied from the air separation equipment 42 . Further, the compressed air extracted from the gas turbine device 7 (to be described later) is pressurized by the booster 68 and then supplied to the gasification furnace equipment 3 through the compressed air supply line 41 together with oxygen supplied from the air separation equipment 42 .

In the gasification furnace equipment 3, the supplied pulverized coal and char are combusted with compressed air (oxygen), and the pulverized coal and char are gasified to generate a generated gas. The produced gas is discharged from the gasification furnace equipment 3 through the produced gas line 49 and sent to the char recovery equipment 11 .

In the char recovery equipment 11, the generated gas is first supplied to the dust collection equipment 51, thereby separating fine char particles contained in the generated gas. The produced gas from which the char has been separated is sent to the gas purification facility 5 through the gas discharge line 53 . On the other hand, the fine char separated from the generated gas is accumulated in the supply hopper 52 and returned to the gasification furnace facility 3 through the char return line 46 for recycling.

The generated gas from which the char is separated by the char recovery equipment 11 is purified by removing impurities such as sulfur compounds and nitrogen compounds in the gas purification equipment 5 to produce fuel gas.

Compressor 61 generates and supplies compressed air to combustor 62 . This combustor 62 mixes the compressed air supplied from the compressor 61 and fuel gas, and combusts them to generate combustion gas. By rotating the gas turbine 63 with this combustion gas, the compressor 61 and the generator 19 are rotated via the rotating shaft 64 . Thus, the gas turbine device 7 can generate power.

The heat recovery steam generator 20 exchanges heat between exhaust gas discharged from the gas turbine 63 (hereinafter referred to as “GT exhaust gas”) and feed water supplied from the condenser 72 to generate steam. The generated steam is supplied to the steam turbine device 18 . The steam turbine device 18 is driven to rotate by the steam supplied from the heat recovery steam generator 20, thereby driving the generator 19 to rotate via the rotating shaft 64, thereby generating power.
It should be noted that the gas turbine device 7 and the steam turbine device 18 do not have to rotate a single generator 19 on the same shaft, and may rotate a plurality of generators on separate shafts.

[Configuration of Singa Cooler and Heat Recovery Boiler]
Next, the configuration of the syngas cooler 35A and the heat recovery boiler 20 will be described in detail.
FIG. 2 shows the syngas cooler 35A, the heat recovery boiler 20, and the pipes (PA1 to PA4, PH1 to PH7, PS1 to PS4) that connect them, which are provided in the gasification facility.

The syngas cooler 35A includes an SGC superheater (product gas heat exchanger) 206, an SGC evaporator (product gas heat exchanger) 204, and an SGC economizer (product gas heat exchanger) 202 (hereinafter referred to as SGC superheater 206, SGC evaporator 204 and SGC economizer 202 are simply referred to as "product gas heat exchangers" when not distinguished). At this time, the SGC economizer 202 is arranged downstream of the SGC superheater 206 and the SGC evaporator 204 in the flow direction of the generated gas. The singa cooler 35A also includes an SGC drum (first drum) 208 as a gas-liquid separator connected to these product gas heat exchangers. In addition, the syngas cooler 35A includes a hanger tube 230 extending vertically and supporting the product gas heat exchanger. At this time, each product gas heat exchanger and suspension pipe 230 are provided in the product gas channel through which the product gas flows, and the SGC drum 208 is provided outside the product gas channel.

The suspension pipe 230 is configured such that cooling water (second water supply) flows therein, thereby suppressing abnormal overheating of the suspension pipe 230 itself.

The product gas heat exchanger and the SGC drum 208 are connected by piping (PS1 to PS4).
Specifically, the water supply outlet of the SGC economizer 202 and the SGC drum 208 are connected by a pipe PS1. The SGC evaporator 204 and the SGC drum 208 are connected by piping PS2 and piping PS3. The steam inlet of SGC superheater 206 and SGC drum 208 are connected by piping PS4.

The exhaust heat recovery boiler 20 includes, in order from the upstream in the flow direction of the GT exhaust gas, a high-pressure superheater (combustion gas heat exchanger) 106, a high-pressure evaporator (combustion gas heat exchanger) 104, a high-pressure secondary economizer (combustion gas heat exchanger) 102 and a high-pressure primary economizer (combustion gas heat exchanger) 101 (hereinafter referred to as a high-pressure superheater 106, a high-pressure evaporator 104, a high-pressure secondary economizer 102, and a high-pressure primary economizer 101 If not, simply referred to as "combustion gas heat exchanger"). The heat recovery steam generator 20 also includes an HRSG drum 108 as a gas-liquid separator connected to these combustion gas heat exchangers. At this time, the combustion gas heat exchanger is provided in the exhaust gas flow path through which the GT exhaust gas flows, and the HRSG drum 108 is provided outside the exhaust gas flow path.

Each combustion gas heat exchanger and the combustion gas heat exchanger and the HRSG drum 108 are connected by pipes (PH1 to PH7).
Specifically, a pipe PH7 is connected to the feed water inlet of the high-pressure primary economizer 101 . The feed water outlet of the high pressure primary economizer 101 and the feed water inlet of the high pressure secondary economizer 102 are connected by a pipe (second pipe) PH2. The feed water outlet of the high-pressure secondary economizer 102 and the HRSG drum 108 are connected by a pipe (first pipe) PH1. The high pressure evaporator 104 and the HRSG drum 108 are connected by pipes PH3 and PH4. The steam inlet of high pressure superheater 106 and HRSG drum 108 are connected by pipe PH5. A pipe PH6 is connected to the steam outlet of the high-pressure superheater 106 .
The high-pressure water supply system of the heat recovery boiler 20, such as the pipes PH1 and PH2, may be provided with an orifice, a valve, or the like for securing the necessary pressure loss.
Further, the other end of the pipe PH7 is connected to a condenser 72 (see FIG. 1), and a high-pressure water supply pump (not shown) provided on the pipe PH7 supplies water from the condenser 72 to the high-pressure primary economizer 101. Water (third water supply) is supplied. The other end of the pipe PH6 is connected to a steam supply line 71 to supply high pressure steam to the steam turbine device 18 .

The water level of the HRSG drum 108 is monitored by a level gauge 112, and based on a signal from the level gauge 112, a controller (not shown) determines the degree of opening of the first flow control valve 110 provided in the pipe PH1. ing.

The syngas cooler 35A and the heat recovery steam generator 20 described above are connected by pipes (PA1 to PA4). Each pipe (PA1 to PA4) will be described in detail below.

The pipe PA1 connects the first water intake portion 141 provided in the pipe PH1 and the feed water inlet of the SGC economizer 202, and extracts part of the third feed water flowing through the pipe PH1 and extracts it as the first feed water from the SGC It is supplied to the economizer 202 .
The first water intake section 141 is provided in the pipe PH1 between the high-pressure secondary economizer 102 and the first flow control valve 110 .

The pipe PA2 connects the second water intake portion 142 provided in the pipe PH2 and the water supply inlet at the lower portion of the suspension pipe 230, and extracts part of the third water supply flowing through the pipe PH2 and suspends it as the second water supply. It feeds down pipe 230 .

A pipe (first water return pipe) PA3 connects the water supply outlet at the top of the suspension pipe 230 and the first water return portion 151 provided in the pipe PH1, and supplies the second water supply discharged from the suspension pipe 230. It is returned to piping PH1.
The first water return section 151 is provided in the pipe PH1 between the high pressure secondary economizer 102 and the first water intake section 141 .

The pipe PA4 connects the steam outlet of the SGC superheater 206 and the pipe PH5, and supplies the steam discharged from the SGC superheater 206 to the high pressure superheater 106 via the pipe PH5.

[Operation of Singa Cooler and Heat Recovery Steam Generator]
Next, the operation of the syngas cooler 35A and the heat recovery boiler 20 will be described in detail.
In the product gas heat exchanger of the syngas cooler 35A and the SGC drum 208, when the high temperature product gas is introduced from the reductor section 33, heat is exchanged between the product gas and the first feed water by the product gas heat exchanger. Steam is generated from the first feed water by the product gas heat exchanger and the SGC drum 208 , superheated, and supplied to the heat recovery boiler 20 .

Specifically, first, first feed water supplied from the heat recovery boiler 20 (pipe PH1) to the SGC economizer 202 via the pipe PA1 is heated by the SGC economizer 202 . The first feed water heated by the SGC economizer 202 is supplied to the SGC drum 208 via the piping PS1. At this time, the water supply outlet of the SGC economizer 202 is set to a subcooling degree (economy subcooling degree) so that steaming in the SGC economizer 202 can be avoided. The first feed water supplied to the SGC drum 208 is supplied to the SGC evaporator 204 via the pipe PS2, and is returned to the SGC drum 208 via the pipe PS3 as the first feed water partially converted to steam. The steam separated into gas and liquid by the SGC drum 208 is supplied to the SGC superheater 206 via the pipe PS4 and superheated, and then supplied to the high-pressure superheater 106 of the heat recovery boiler 20 via the pipe PA4 and the pipe PH5. be done.

In the suspension pipe 230 of the syngas cooler 35A, when the high-temperature generated gas is introduced from the reductor portion 33 to the syngas cooler 35A, heat exchange is performed between the generated gas and the second feed water by the suspension pipe 230, and the second The feed water is heated.

Specifically, first, the second feedwater supplied from the heat recovery boiler 20 (pipe PH2) to the suspension pipe 230 through the pipe PA2 is heated by the suspension pipe 230, and then through the pipe PA3. The water is returned to the first water return section 151 provided in PH1 and mixed with the third water supply flowing through the pipe PH1. At this time, a subcooling degree (suspension pipe subcooling degree) is set at the water supply outlet of the suspension pipe 230 so that steaming in the suspension pipe 230 can be avoided.
Moreover, the suspension pipe 230 suppresses abnormal overheating of the suspension pipe 230 by the second water supply. That is, the suspension pipe 230 is responsible for heating the second feed water, supporting the product gas heat exchanger, and preventing abnormal overheating. At this time, since the main purpose of the second water supply flowing through the suspension pipe 230 is to prevent abnormal overheating, it is preferable that the flow rate of the second water supply is constant.

Here, the high-temperature generated gas led to the syngas cooler 35A has a temperature of 1000° C. or higher and 1200° C. or lower near the inlet of the syngas cooler 35A, and a temperature of 300° C. or higher and 500° C. or lower near the outlet.

In the heat recovery boiler 20, when the high-temperature GT exhaust gas is introduced from the gas turbine 63, heat is exchanged between the GT exhaust gas and the third feed water by the combustion gas heat exchanger. Steam is then produced from the third feed water by the combustion gas heat exchanger and HRSG drum 108 .

Specifically, first, the third water supply supplied from the condenser 72 to the high-pressure primary economizer 101 via the pipe PH7 is cooled to, for example, 200° C. or higher and 300° C. or lower by the high-pressure primary economizer 101. It is heated to a first predetermined temperature (predetermined temperature). The third water supply heated by the high-pressure primary economizer 101 is supplied to the high-pressure secondary economizer 102 through the pipe PH2 and further heated to reach the second predetermined temperature. The third feedwater heated by the high-pressure secondary economizer 102 is supplied to the HRSG drum 108 through the pipe PH1. The third feedwater supplied to the HRSG drum 108 is supplied to the high-pressure evaporator 104 via the pipe PH3, and is returned to the HRSG drum 108 via the pipe PS4 as the third feedwater partially converted to steam. The steam separated into gas and liquid by the HRSG drum 108 is supplied to the high-pressure superheater 106 through the pipe PH5 to be superheated, and then supplied to the steam supply line 71 through the pipe PH6.

Here, it is preferable that the second predetermined temperature of the third feed water after being heated by the high-pressure secondary economizer 102 is higher than that of the second feed water returned to the first water return section 151 . Accordingly, even if the third water supply having the second predetermined temperature and the second water supply are mixed, the temperature of the third water supply after mixing is at least higher than that of the second water supply returned to the first water return section 151 . Become.

According to this embodiment, the following effects are obtained.
That is, the second water supply is taken out from the third water supply of a predetermined temperature that flows through the pipe PH2, and the first water supply is taken out from the third water supply that flows through the pipe PH1. At this time, the third feed water at the first predetermined temperature is heated to the second predetermined temperature (>first predetermined temperature) by the high-pressure secondary economizer 102 . Further, the second water supply flowing out from the suspension pipe 230 is returned to the first water return portion 151 provided in the pipe PH1.
By this, the 2nd water supply heated by the hanging pipe 230 can be set as the structure which is not directly led|guided to the SGC economizer 202 which the singa cooler 35A has as 1st water supply. Therefore, even if the suspension pipe subcooling degree is set for the second water supply flowing out from the suspension pipe 230, the suspension pipe subcooling degree does not limit the temperature of the first water supply. That is, in order to make the temperature of the water supply for the SGC economizer 202 optimal, the temperature of the first water supply supplied to the SGC economizer 202 is set to be higher than the temperature of the second water supply heated by the suspension pipe 230. can do. The "optimum temperature" referred to here is the temperature (depending on the pressure, 300° C. or higher and 350° C. or lower as an example). By doing so, the temperature difference between the temperature of the produced gas (300° C. or higher and 500° C. or lower near the installation position of the SGC economizer 202) and the first feed water temperature can be reduced, so the steam in the syngas cooler 35A The amount generated can be increased. That is, the heat (sensible heat) of the generated gas can be efficiently used. In addition, since it is possible to suppress the generated gas from being cooled more than necessary, it is possible to avoid a phenomenon in which the temperature of the generated gas after heat exchange falls below the temperature required for purification (for example, the catalyst activation temperature in the COS converter 21). .

The first water supply is the third water supply obtained by mixing the third water supply at the second predetermined temperature and the second water supply heated by the suspension pipe 230 .
Thereby, the total flow rate of the flow rate of the third water supply flowing through the pipe PH1 and the flow rate of the second water supply returned from the suspension pipe 230 can be secured as the flow rate that can be supplied to the first water supply.

In addition, for example, it may be configured such that the third feed water is supplied to an auxiliary boiler (boiler) provided in the gasification facility. In this case, the gasification equipment does not have to be equipped with the heat recovery steam generator 20 .

[Second embodiment]
Hereinafter, a gasification facility according to a second embodiment of the present invention and an integrated gasification combined cycle facility having the same will be described with reference to the drawings. This embodiment is different from the first embodiment in that the destination of the second water supply is the SGC drum 208 and the SGC economizer 202 is replaced with the SGC second evaporator 210 . Therefore, in the following description, the same reference numerals are given to the same configurations as in the first embodiment, and the different configurations will be described.

[Configuration of Singa Cooler and Heat Recovery Boiler]
FIG. 3 shows a syngas cooler 35B, an exhaust heat recovery boiler 20, and pipes (PA1 to PA4, PH1 to PH7, PS2 to PS6) connecting them, which are provided in gasification equipment.

The syngas cooler 35B includes an SGC superheater (product gas heat exchanger) 206, an SGC evaporator (product gas heat exchanger) 204, and an SGC second evaporator (product gas heat exchanger) 210 (hereinafter referred to as SGC When the superheater 206, the SGC evaporator 204 and the SGC secondary evaporator 210 are not distinguished, they are simply referred to as "product gas heat exchangers"). At this time, the SGC second evaporator 210 is arranged downstream of the SGC superheater 206 and the SGC evaporator 204 in the flow direction of the produced gas. The singa cooler 35B also includes an SGC drum 208 as a gas-liquid separator connected to these product gas heat exchangers. Furthermore, the singa cooler 35B has a suspension pipe 230 extending along the vertical direction. At this time, the product gas heat exchanger and suspension pipe 230 are provided in the product gas channel through which the product gas flows, and the SGC drum 208 is provided outside the product gas channel.

The SGC second evaporator 210 and the SGC drum 208 are connected by a pipe PS5 and a pipe PS6.

The pipe PA1 connects the first water intake portion 141 provided in the pipe PH1 and the SGC drum 208, and part of the third water supply flowing through the pipe PH1 is taken out and supplied to the SGC economizer 202 as the first water supply. are supplying.

[Operation of Singa Cooler and Heat Recovery Steam Generator]
Next, operations of the syngas cooler 35B and the heat recovery boiler 20 will be described in detail.
First, the first feed water taken out from the heat recovery boiler 20 (pipe PH1) is supplied to the SGC drum 208 through the pipe PA1. The first feed water supplied to the SGC drum 208 is supplied to the SGC evaporator 204 via the pipe PS2, and is returned to the SGC drum 208 via the pipe PS3 as the first feed water partially converted to steam. In addition, the first water supply supplied to the SGC drum 208 is supplied to the SGC second evaporator 210 through the pipe PS5, and is returned to the SGC drum 208 through the pipe PS6 as the first water supply partially converted to steam. be The steam separated into gas and liquid by the SGC drum 208 is supplied to the SGC superheater 206 via the pipe PS4 and superheated, and then supplied to the high-pressure superheater 106 of the heat recovery boiler 20 via the pipe PA4 and the pipe PH5. be done.

According to this embodiment, the following effects are obtained.
That is, the first feed water taken out from the heat recovery boiler 20 (pipe PH1) is supplied to the SGC drum 208 via the pipe PA1.
This allows the first feed water to be supplied directly to the SGC drum 208, so compared to the case where the first feed water is supplied to the economizer (see, for example, the SGC economizer 202 of the first embodiment) , the temperature of the first feed water can be made higher. Also, steam can be efficiently generated by the SGC evaporator 204 and the SGC second evaporator 210 .

[Modification 1]
As shown in FIG. 4, in the above-described first and second embodiments, the configuration around the first flow control valve 110, the first water intake section 141, and the first water return section 151 is similar to that in the pipe PH1. The first water return section 151, the first water intake section 141, and the first flow control valve 110 are arranged in this order from the upstream side along the direction of circulation of the third water supply.

As shown in FIG. 5, this configuration may be arranged in the order of the first water intake section 141, the first water return section 151, and the first flow control valve 110 from the upstream side.
Thereby, the first water supply can be the third water supply before being mixed with the second water supply returned from the suspension pipe 230 . At this time, the third water supply is kept at the second predetermined temperature. Therefore, the temperature of the first water supply is lower than when the third water supply, which is a mixture of the third water supply at the second predetermined temperature and the second water supply heated by the suspension pipe 230, is used as the first water supply. can be avoided.

[Modification 2]
As shown in FIG. 6, the first water intake section 141, the first flow control valve 110, and the first water return section 151 may be arranged in this order from the upstream side.
Thereby, the flow rate of the second water supply flowing through the suspension pipe 230 can be ensured. In this case, the first flow control valve 110 acts as a valve that secures the pressure loss necessary for the high-pressure water supply system of the heat recovery boiler 20 .

[Third Embodiment]
Hereinafter, a gasification facility according to a third embodiment of the present invention and an integrated gasification combined cycle facility having the same will be described with reference to the drawings. This embodiment differs from the first embodiment and the second embodiment in that a pipe PA5 is provided in the pipe PA3. Therefore, in the following description, the same reference numerals are given to the same configurations as in the first and second embodiments, and the different configurations will be described.

FIG. 7 shows a syngas cooler 35C, an exhaust heat recovery boiler 20, and pipes (PA1 to PA5, PH1 to PH7, PS1 to PS4) connecting them, which are provided in a gasification facility.

The singa cooler 35C includes an SGC superheater 206, an SGC evaporator 204, and an SGC economizer 202, as in the first embodiment (see FIG. 2). The singa cooler 35C also includes an SGC drum 208 as a gas-liquid separator connected to these product gas heat exchangers.
In addition, it is good also as a structure which replaced with the SGC economizer 202 and provided the SGC 2nd evaporator 210 like 2nd Embodiment (refer FIG. 3).

A second flow control valve 212 and a flow meter 216 are provided in the pipe PA3. Thereby, the flow rate of the second water supply flowing through the pipe PA3 can be adjusted. As a result, the flow rate of the second water supply flowing through the suspension pipe 230 can be adjusted. The degree of opening of the second flow control valve 212 is determined by a controller (not shown) based on a signal from the flowmeter 216. FIG.

A pipe (branch pipe) PA5 is connected to the pipe PA3. The other end of the pipe PA5 is connected to a flush pipe and a condenser 72, so that the second water supply flowing through the pipe PA3 can be discharged to the outside of the system.

A third flow control valve 214 is provided in the pipe PA5. The degree of opening of the third flow control valve 214 is determined by a controller (not shown) based on a signal from the flowmeter 216. FIG.

According to this embodiment, the following effects are obtained.
That is, the pipe PA3 is provided with the second flow control valve 212 . Thereby, the flow rate of the second water supply flowing through the suspension pipe 230 can be adjusted.

Moreover, the 3rd flow control valve 214 is provided in piping PA5 connected to piping PA3. The third flow control valve 214 is used in the following cases. That is, when the flow rate of the second water supply is insufficient even though the degree of opening of the second flow rate adjustment valve 212 is fully open, the degree of opening of the third flow rate adjustment valve 214 is increased to increase the degree of opening of the second water supply. ensure the flow rate of When the flow rate of the second water supply can be adjusted only by adjusting the opening degree of the second flow rate adjustment valve 212, the opening degree of the third flow rate adjustment valve 214 is kept constant (for example, fully closed).

Further, when the flow rate of the second feed water is large with respect to the amount of steam generated by the heat recovery boiler 20 or the syngas cooler 35, excess second feed water can be discharged outside the system through the pipe PA5.

[Fourth embodiment]
Hereinafter, a gasification facility according to a fourth embodiment of the present invention and an integrated gasification combined cycle facility having the same will be described with reference to the drawings. This embodiment differs from the first to third embodiments in that the water return destination of the pipe PA3 is the pipe PH2. Therefore, in the following description, the same reference numerals are given to the same configurations as in the first to third embodiments, and the different configurations will be described.

FIG. 8 shows a syngas cooler 35D, an exhaust heat recovery boiler 20, and pipes (PA1 to PA4, PH1 to PH7, PS1 to PS4) connecting them, which are provided in a gasification facility.

The singa cooler 35D includes an SGC superheater 206, an SGC evaporator 204, and an SGC economizer 202, as in the first embodiment (see FIG. 2). The singa cooler 35D also includes an SGC drum 208 as a gas-liquid separator connected to these product gas heat exchangers.
In addition, it is good also as a structure which replaced with the SGC economizer 202 and provided the SGC 2nd evaporator 210 like 2nd Embodiment (refer FIG. 3).

The pipe PA3 connects the water supply outlet at the top of the suspension pipe 230 and the second water return portion 152 provided in the pipe PH2, and returns the second water supply discharged from the suspension pipe 230 to the pipe PH2. . At this time, the second water return section 152 is located upstream of the second water intake section 142 in the flow direction of the third water supply of the pipe PH2.
Thereby, the second water supply can be circulated through the pipe PA2, the suspension pipe 230, the pipe PA3, and the pipe PH2 (the pipe PH2 between the second water return section 152 and the second water intake section 142).

A water pump 232 is provided in the pipe PA2. This makes it possible to ensure the pressure head necessary for circulation of the secondary water supply.

According to this embodiment, the following effects are obtained.
That is, the second water supply is circulated by the pipe PA2, the suspension pipe 230, the pipe PA3, the pipe PH2, and the water pump 232.
As a result, the flow rate of the second water supply is adjusted by the water pump 232 . Therefore, for example, even when the integrated gasification combined cycle facility is not in rated operation, that is, even when the amount of steam generated by the heat recovery steam generator 20 or the syngas cooler 35 is less than that during rated operation, a certain amount of second feed water is supplied. It can be circulated in the suspension pipe 230 .

[Fifth embodiment]
Hereinafter, a gasification facility according to a fifth embodiment of the present invention and an integrated gasification combined cycle facility having the same will be described with reference to the drawings. The present embodiment differs from the first to fourth embodiments in that the pipe PA3 is returned to the SGC drum 208 . Therefore, in the following description, the same reference numerals are given to the same configurations as in the first to fourth embodiments, and the different configurations will be described.

FIG. 9 shows a syngas cooler 35E, an exhaust heat recovery boiler 20, and pipes (PA1 to PA4, PH1 to PH7, PS1 to PS4) connecting them, which are provided in gasification equipment.

The singa cooler 35E includes an SGC superheater 206, an SGC evaporator 204, and an SGC economizer 202, as in the first embodiment (see FIG. 2). The singa cooler 35D also includes an SGC drum 208 as a gas-liquid separator connected to these product gas heat exchangers.
In addition, it is good also as a structure which replaced with the SGC economizer 202 and provided the SGC 2nd evaporator 210 like 2nd Embodiment (refer FIG. 3).

A pipe PA3 connects the water supply outlet at the top of the suspension pipe 230 and the SGC drum 208, and returns the second water supply discharged from the suspension pipe 230 to the SGC drum 208.

According to this embodiment, the following effects are obtained.
That is, the second water supply is taken out from the third water supply of a predetermined temperature that flows through the pipe PH2, and the first water supply is taken out from the third water supply that flows through the pipe PH1. At this time, the second water supply flowing out from the suspension pipe 230 is returned to the SGC drum 208 .
Thereby, the second water supply heated by the suspension pipe 230 can be led to the SGC drum 208 as a water supply system separate from the first water supply. Therefore, even if the suspension pipe subcooling degree is set for the second water supply flowing out from the suspension pipe 230, the suspension pipe subcooling degree does not limit the temperature of the first water supply. That is, the first feed water temperature can be set to the optimum temperature for the SGC economizer 202 and the SGC drum 208 of the syngas cooler 35 . By doing so, the temperature difference between the temperature of the produced gas and the temperature of the first feed water can be reduced, so that the amount of steam generated in the syngas cooler 35A can be increased. That is, the heat (sensible heat) of the generated gas can be efficiently used. In addition, since it is possible to suppress the generated gas from being cooled more than necessary, it is possible to avoid a phenomenon in which the temperature of the generated gas after heat exchange falls below the temperature required for purification (for example, the catalyst activation temperature in the COS converter 21). .

It should be noted that the configurations of the first to fifth embodiments can be combined within a possible range, and can be appropriately designed according to the specifications of the facility.

1 coal gasification combined cycle facility 16 gasification furnace 20 exhaust heat recovery boiler (boiler)
35 Singa cooler (produced gas heat exchange part)
63 gas turbine 101 high-pressure primary economizer (one combustion gas heat exchanger)
102 High pressure secondary economizer (other combustion gas heat exchanger)
104 high pressure evaporator (combustion gas heat exchanger)
106 high-pressure superheater (combustion gas heat exchanger)
110 First flow control valve 141 First water intake section 142 Second water intake section 151 First water return section 152 Second water return section 202 SGC economizer (produced gas heat exchanger)
204 SGC evaporator (product gas heat exchanger)
206 SGC superheater (product gas heat exchanger)
208 SGC drum (first drum)
210 SGC second evaporator (product gas heat exchanger)
212 Second flow control valve 214 Third flow control valve 230 Suspended pipe 232 Water pump PA3 Piping (first return pipe)
PA5 piping (branch piping)
PH1 pipe (1st pipe)
PH2 pipe (second pipe)

Claims (13)

a product gas heat exchange unit having a plurality of product gas heat exchangers and a first drum for separating steam into gas and liquid, wherein the product gas produced from the carbon-containing solid fuel heats the first feedwater to produce steam; a suspension pipe supporting a plurality of the product gas heat exchangers and having a second feed water flow therein;
a boiler that heats the third feed water to generate steam;
with
The second water supply is taken from the third water supply at a predetermined temperature,
The first feed water is taken from the third feed water heated by the boiler to a temperature higher than the predetermined temperature. one of the plurality of product gas heat exchangers is an economizer that heats water,
2. The gasification facility according to claim 1, wherein said first feed water is supplied to said economizer. One of the plurality of product gas heat exchangers is an evaporator that evaporates water,
The first drum separates the vapor generated by the evaporator into gas and liquid,
2. The gasification facility according to claim 1, wherein said first feed water is supplied to said first drum. The boiler has one combustion gas heat exchanger and another combustion gas heat exchanger,
The third feed water is led to the one combustion gas heat exchanger and the other combustion gas heat exchanger in this order,
The one combustion gas heat exchanger is installed downstream of the other combustion gas heat exchanger in the flow direction of the combustion gas,
The first feed water is taken from the third feed water flowing through a first pipe connected to the outlet of the other combustion gas heat exchanger,
The second water supply is taken out from the third water supply flowing through a second pipe connecting the outlet of the one combustion gas heat exchanger and the inlet of the other combustion gas heat exchanger. 4. The gasification facility according to any one of 1 to 3. The first water supply is taken out from the first water intake portion of the first pipe,
The second water supply flowing out of the suspension pipe is supplied to a first water return portion provided in the first pipe on the upstream side of the first water intake portion in the flow direction of the third water supply in the first pipe. 5. The gasification facility of claim 4, wherein the gasification facility is returned to the The first water supply is taken out from the first water intake portion of the first pipe,
5. The second water supply that has flowed out of the suspension pipe is returned to a first water return section downstream of the first water intake section in the flow direction of the third water supply in the first pipe. The gasification facility described in . A first flow control valve is provided in the first pipe downstream of the first water intake section in the direction of flow of the third water supply in the first pipe,
7. The gasification facility according to claim 6, wherein said first water return section is provided downstream of said first flow control valve in the direction of flow of said third water supply in said first pipe. A first water return pipe is provided between the outlet of the suspension pipe and the first water return section,
8. The gasification facility according to any one of claims 5 to 7, wherein the first return pipe is provided with a second flow control valve. A branch pipe is connected to the first water return pipe on the upstream side of the second flow control valve in the flow direction of the second water supply in the first water return pipe,
9. The gasification facility according to claim 8, wherein the branch pipe is provided with a third flow control valve. A water pump for sending the second water supply to the suspension pipe,
The second water supply is taken out from the second water intake portion of the second pipe,
The second water supply flowing out of the suspension pipe is supplied to a second water return portion provided in the second pipe upstream of the second water intake portion in the flow direction of the third water supply in the second pipe. 5. The gasification facility of claim 4, wherein the gasification facility is returned to the 5. The gasification facility according to any one of claims 1 to 4, wherein said second water supply flowing out of said suspension pipe is fed to said first drum. The gasification facility according to any one of claims 1 to 11, wherein the boiler is an exhaust heat recovery boiler that heats the third feed water with exhaust gas from a gas turbine to generate steam. An integrated gasification combined cycle facility comprising the gasification facility according to any one of claims 1 to 12.

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