JP6057362B1 - Supercritical water gasification system - Google Patents

Abstract

In the present invention, it comprises a heat treatment part for heating and gasifying a slurry body prepared from biomass in a raw material preparation part, and a gas treatment part for extracting fuel gas from a supercritical high-temperature fluid sent from the heat treatment part, The heat treatment section includes a gasification reactor that generates a supercritical high-temperature fluid by heating and gasifying the slurry body. In the gasification reactor, the slurry body sent from the raw material preparation section is heated to a gasification reaction temperature at which gasification is possible, and the organic matter contained in the slurry body is hydrothermally treated. That is, since the slurry body is heated and gasified to a high temperature and high pressure condition at once in the gasification reactor, the slurry body can be efficiently heated. Thereby, since it is not necessary to provide the heat exchanger for preheating in the front | former stage of a gasification reactor, the production | generation of a tar and char can be suppressed, As a result, gasification of biomass can be performed efficiently. .

Description

  The present invention relates to a supercritical water gasification system that generates a fuel gas by decomposing a slurry body produced by preparing biomass in a supercritical state.

  A supercritical water gasifier that obtains fuel gas by decomposing biomass in a supercritical state is known. For example, Patent Document 1 discloses that a biomass slurry containing a nonmetallic catalyst is hydrothermally treated under conditions of a temperature of 374 ° C. or higher and a pressure of 22.1 MPa or higher, and the generated fuel gas is used for a power generator. A biomass gasification power generation system that generates power and heats a slurry body using exhaust heat from a power generation device is described.

JP 2008-246343 A

  FIG. 9 is a diagram illustrating a general biomass gasification power generation system. As shown in the figure, the gasification system 2 includes a heat exchanger 3, a heater 4, and a gasification reactor 5. Among these parts, the heat exchanger 3 is a device for heating the slurry-like raw material (slurry body). This slurry body is prepared, for example, by adding water and activated carbon (catalyst) to biomass such as shochu residue, egg-collecting chicken manure, sludge and the like and mixing them. The heater 4 is a device that raises the temperature of the slurry heated by the heat exchanger 3 to a gasification reaction temperature (temperature at which the slurry is gasified (gasification is possible)). The gasification reactor 5 is an apparatus that keeps the slurry body constant at the gasification reaction temperature. The fluid that has undergone the gasification reaction is then gas-liquid separated, and the gas component is used as fuel gas.

  Here, as the heat exchanger 3, for example, a double-pipe heat exchanger is used. FIG. 10 is a diagram illustrating the configuration of the double pipe 6 provided in the double pipe heat exchanger. As shown in the figure, in the double pipe 6, a low-temperature flow path 8 is defined inside the inner pipe 7, and a high-temperature flow path 11 is defined between the outer pipe 9 and the inner pipe 7. A slurry body 13 is circulated through the low temperature flow path 8. A high-temperature fluid 14 that exchanges heat with the slurry body 13 is circulated in the high-temperature channel 11 in a direction opposite to the slurry body 13. Then, the slurry body 13 introduced from the inlet 12 of the low-temperature channel 8 is heated while exchanging heat with the high-temperature fluid 14 and discharged from the outlet 15.

  FIG. 11 is a diagram illustrating an example of a temperature change of the slurry body 13 and a temperature change of the high-temperature fluid 14 in the heat exchanger 3 including the double pipe 6. In the figure, the vertical axis indicates the temperature of the fluid, and the horizontal axis indicates the distance of the double pipe 6. Supplementing the distance of the double pipe 6, the distance of the double pipe 6 from the inlet 12 when the position of the inlet 12 in the inner pipe 7 is 0 and the position of the outlet 15 is 100 is shown. Distance.

  As shown in the figure, the temperature of the slurry 13 (see FIG. 10) introduced into the inlet 12 at normal temperature is raised, but the intermediate portion 16 of the heat exchanger 3 (the temperature of the slurry 13 is about 380 ° C.). In the portion where the distance from the inlet 12 is about 30 to about 70), it can be seen that the temperature increase rate of the slurry 13 is extremely slow. Similarly, with respect to the high temperature fluid 14 (see FIG. 10), almost no temperature change is observed in the intermediate portion 16, and the temperature is about 380 ° C. which is substantially the same as that of the slurry body 13.

  Thus, the reason why the temperature change of the slurry body 13 and the high-temperature fluid 14 in the intermediate portion 16 is smaller than that of the other portions is that the constant pressure specific heat of the slurry body 13 and the high-temperature fluid 14 in the intermediate portion 16 is high. It is thought that it is because.

  That is, the internal pressure of the heat exchanger 3 is a high pressure (for example, 25 MPa), but under such a high pressure, the constant pressure specific heat of the slurry body 13 and the high temperature fluid 14 is a specifically high peak near the critical temperature (about 380 ° C.). It is known to take a value. Actually, the constant pressure specific heat of the high temperature fluid 14 peaks at a temperature slightly lower than the constant pressure specific heat of the slurry body 13 due to pressure loss in the double pipe 6. For this reason, the temperature difference between the slurry body 13 and the high temperature fluid 14 is minimized in the intermediate portion 16, and the heat exchange amount per unit heat transfer area is a portion other than the intermediate portion, and the low temperature portion 17 and the high temperature of the heat exchanger 3. Smaller than the portion 18. As a result, the slurry body 13 is in a state where it is difficult to raise the temperature.

  Further, it is known that tar derived from biomass components is easily generated in the intermediate portion 16. The generated tar adheres to the inner wall of the inner pipe 7 to reduce the heat passage rate, and closes the pipe, thereby obstructing the flow of the slurry body 13 and further reducing the exchange heat per unit heat transfer area. It has become.

  Accordingly, the present invention has been made in view of such a current situation, and an object thereof is to provide a supercritical water gasification system capable of efficiently gasifying biomass by suppressing the generation of tar and char. And

In order to solve the above problems, a supercritical water gasification system according to the present invention is:
A gasification system for generating fuel gas by decomposing a slurry body produced by preparing biomass in a supercritical state,
A raw material preparation unit for preparing the slurry body from the biomass;
A heat treatment part for heating and gasifying the slurry body prepared in the raw material preparation part;
A gas processing unit for extracting fuel gas from a supercritical high-temperature fluid sent from the heat treatment unit,
The heat treatment section includes a gasification reactor that generates the supercritical high-temperature fluid by heating and gasifying the slurry body,
A part or all of the high-temperature fluid is used as a heat source for heating other than direct heating of the slurry body ,
The biomass comprises a shochu residue, further comprising a dryer for drying the shochu residue,
The dryer is characterized by drying the shochu residue using exhaust heat generated when the high-temperature fluid is generated in the gasification reactor .

In the supercritical water gasification system of the present invention,
The gas processing unit has a heat exchanger in which the supercritical high-temperature fluid is introduced and heat-exchanges the high-temperature fluid and pure water.
In the gasification reactor, the slurry body sent from the raw material preparation unit is heated to a gasification reaction temperature at which gasification is possible, and the organic matter contained in the slurry body is hydrothermally treated,
In the heat exchanger, it is preferable to heat the pure water by exchanging heat between the high-temperature fluid generated by the gasification reactor and pure water to generate steam and to cool the high-temperature fluid. .

  At this time, the heat exchanger may be a cooling tank in which pure water is stored.

Furthermore, in the supercritical water gasification system of the present invention,
The heat treatment unit may further include a heat exchanger that preheats the slurry body prepared in the raw material preparation unit using exhaust heat of the gasification reactor.

In the supercritical water gasification system of the present invention,
The gasification reactor is
The product gas extracted from the product produced by the gasification process may be used as a fuel.

Furthermore, in the supercritical water gasification system of the present invention,
The gas processing unit,
Said steam, said product gas effluent from the heat engine of another system for use as a fuel and is heat exchanged may further comprise a heat exchanger for discharging as exhaust gas.

  According to the present invention, the production of tar and char can be suppressed and biomass can be efficiently gasified.

BRIEF DESCRIPTION OF THE DRAWINGS It is a figure which shows schematic structure of the supercritical water gasification system demonstrated as 1st Embodiment of this invention. It is a figure which shows the modification in the supercritical water gasification system of FIG. It is a graph which shows the relationship between the temperature in water, a pressure, and a constant pressure specific heat. It is a figure which shows schematic structure of the supercritical water gasification system demonstrated as 2nd Embodiment of this invention. It is a figure which shows the modification in the supercritical water gasification system of FIG. It is a figure which shows schematic structure of the supercritical water gasification system demonstrated as 3rd Embodiment of this invention. It is a figure which shows the modification in the supercritical water gasification system of FIG. It is a figure which shows the modification in the supercritical water gasification system of FIG. It is a figure which shows the modification in the supercritical water gasification system of FIG. It is a figure explaining a general biomass gasification power generation system. It is a figure explaining the structure of the double pipe in a double pipe type heat exchanger. Illustrated temperature change of hot fluid and slurry body in double tube heat exchanger

  Hereinafter, an embodiment of a supercritical water gasification system according to the present invention will be described. In the following description, the “supercritical water gasification system” is simply referred to as “gasification system”.

  First, the first embodiment will be described. FIG. 1 is a diagram illustrating a configuration of a gasification system 10 according to the first embodiment. In the gasification system 10, a slurry body is prepared from biomass such as shochu residue, egg-collecting chicken manure, and sludge as raw materials, and combustion gas is generated by heating and pressurizing the prepared slurry body. As shown in the figure, the gasification system 10 includes a raw material preparation unit 20, a heat treatment unit 30, and a gas processing unit 40.

  The raw material preparation unit 20 is a part that prepares a slurry body from biomass. The raw material preparation unit includes an adjustment tank 21, a crusher 22, and a gasification reactor introduction pump 24.

  The adjustment tank 21 is a container for mixing biomass, water, and activated carbon which is a kind of gasification catalyst (non-metallic catalyst). Here, hydrous biomass in which water is previously mixed with biomass may be used. In the adjustment tank 21, a mixture in which biomass, water, and activated carbon are mixed is prepared. For example, porous particles having an average particle diameter of 200 μm or less are used as the activated carbon. The mixing ratio of biomass, water, and activated carbon is appropriately adjusted according to the type, amount, moisture content, and the like of biomass.

  The crusher 22 is an apparatus for crushing the solid content of the mixture prepared in the adjustment tank 21 to obtain a uniform size (preferably an average particle size of 500 μm or less, more preferably an average particle size of 300 μm or less). is there. By processing with this crusher 22, a mixture turns into a slurry-form slurry body.

  The gasification reactor introduction pump 24 pressurizes the slurry body sent from the crusher 22 and supplies it to the heat treatment unit 30. The slurry body is pressurized to about 0.1 to 4 MPa by the gasification reactor introduction pump 24.

  The heat treatment unit 30 is a part that heats and gasifies the slurry body prepared by the raw material preparation unit 20. The heat treatment unit 30 includes a gasification reactor 31 and a combustion air fan 32.

  The gasification reactor 31 heats the slurry body sent from the raw material preparation unit 20 to the gasification reaction temperature (temperature at which the slurry body is gasified (gasification is possible)), and organic substances contained in the slurry body Is a device for hydrothermal treatment. The gasification reactor 31 includes a combustion device 31a. The combustion device 31a introduces air sent from a combustion air fan 32 into liquefied petroleum gas (LPG) such as propane gas, coal, petroleum, and the like, and burns it. The slurry body is hydrothermally treated. In this hydrothermal treatment, the slurry body is hydrothermally treated for 1 to 2 minutes under conditions of, for example, 600 ° C. and 25 MPa. The hydrothermally treated slurry body undergoes a gasification reaction, and is then sent as a post-treatment fluid to the gas processing unit 40 (specifically, a high-temperature channel 45 of a heat exchanger 41 described later).

  The gas processing unit 40 is a part that extracts fuel gas from a supercritical high-temperature fluid (fluid after gasification processing) sent from the gasification reactor 31. The gas processing unit 40 includes a heat exchanger 41 that functions as a cooling mechanism, a decompression mechanism 42, a gas-liquid separator 43, and a feed water pump 44.

  The heat exchanger 41 is a device that exchanges heat between the high-temperature fluid sent from the gasification reactor 31 and water. The heat exchanger 41 is a double tube heat exchanger having a double tube, and includes a high temperature channel 45 and a low temperature channel 46. The high-temperature channel 45 is introduced with a supercritical high-temperature fluid (hereinafter also referred to as a post-treatment fluid) generated in the gasification reactor 31, and the post-treatment fluid flows. Water (pure water) sent from the water supply pump 44 is introduced into the low temperature channel 46, and this pure water circulates. Then, the post-treatment fluid that flows through the high-temperature channel 45 and the pure water that flows through the low-temperature channel 46 are heat-exchanged to generate power steam. That is, the heat exchanger 41 functions as a cooling mechanism that cools the processed fluid with pure water.

  The steam for power generated by the heat exchanger 41 is used for various engines using steam of other systems such as a generator using a steam turbine (not shown), a shochu production line, heating of hydrous biomass, and heating of combustion air. It is done. For example, such a power generation system using steam as a power source includes a system including a steam turbine, a generator, a condenser, and a pump. Here, the steam turbine is a device that performs work (rotational motion) with the power steam generated by the heat exchanger 41. The generator is a device that generates electricity by rotating a steam turbine. A condenser is a device that condenses water vapor that has finished work in a steam turbine. The pump is a device that sends water obtained by aggregation to the heat exchanger 41. In such a power generation system, the steam turbine is caused to work by the power steam generated in the heat exchanger 41 (the low temperature channel 46), and electric power is obtained from the generator. And the water vapor | steam which finished work is condensed with a condenser, and the steam for power is produced | generated by sending out the obtained water to the heat exchanger 41. FIG.

  The decompression mechanism 42 is a device that decompresses the processed fluid sent from the heat exchanger 41. The gas-liquid separator 43 converts the processed fluid cooled by the heat exchanger 41 introduced via the decompression mechanism 42 into a liquid (a liquid containing activated carbon or ash) and a gas (a gas such as hydrogen or methane). It is a device that separates into Among these, a part of the liquid (activated carbon) is sent to the adjustment tank 21 and reused, and the remaining part is treated as drainage. In addition, gas is sent to various engines that use fuel gas of different systems, such as generators using internal combustion engines such as gas turbines and gas engines (not shown), and steam generators such as boilers, and used as power generation and power sources. be able to. A part of the gas (product gas) separated by the gas-liquid separator 43 is supplied to the gasification reactor 31 as shown in FIG. May be consumed.

  FIG. 3 is a graph showing the relationship between temperature, pressure, and constant pressure specific heat in water. From this graph, it can be seen that, under ultra-high pressure, the constant pressure specific heat in a specific temperature range (a range of about 370 ° C. to about 400 ° C.) called a pseudocritical point rapidly increases. And the slurry body which contains water as a main component also has the same characteristic.

  In this gasification system 10, since the slurry body is heated and gasified to a high temperature and high pressure (600 ° C., 25 MPa) at once in the gasification reactor 31, the slurry body is efficiently heated to 600 ° C. can do. Thereby, since it is not necessary to provide the heat exchanger for preheating in the front | former stage of the gasification reactor 31, the production | generation of tar and char can be suppressed, As a result, gasification of biomass can be performed efficiently. it can. In addition, the pure water is heated by the heat transferred from the treated fluid to the pure water, generating power vapor and cooling the treated fluid. That is, it is possible to generate steam for power of about a dozen MPa that is used in various engines of different systems by utilizing a portion that becomes exhaust heat in the thermal energy of the processed fluid.

  As described above, in the gasification system 10, a part or all of the treated fluid, which is a high-temperature fluid generated in the gasification reactor 31, is heated (for example, heat exchange) other than direct heating of the slurry body. The steam 41 is used as a heat source for the purpose. In addition, as a heat source for the purpose of heating other than direct heating of the slurry body, for example, biomass can be obtained using exhaust heat generated when a high-temperature fluid is generated in the gasification reactor 31. Various heat sources such as a heat source for producing a dry feed by drying can be widely applied.

  Next, a second embodiment will be described with reference to FIG. 4 in which parts corresponding to those in FIG. As shown in the figure, the gasification system 10 according to the second embodiment is the gasification system of the first embodiment described above except that a plurality of heat exchangers 50 to 53 are newly provided. 10 is configured in substantially the same manner. Therefore, here, for the sake of convenience, different parts will be described, and detailed description of other overlapping parts will be omitted.

  Specifically, the heat exchanger 50 provided in the gasification system 10 according to the second embodiment includes a slurry body prepared and sent by the raw material preparation unit 20 and a heat exchanger 52 described later. The slurry is preheated by exchanging heat with the exhaust gas of the gasification reactor 31 to be introduced. The heat exchanger 51 uses the high-temperature exhaust discharged from various engines of different systems that use the fuel gas separated by the gas-liquid separator 43 to generate the steam generated by the heat exchanger 41. Heat. In other words, the heat exchanger 51 includes the high-temperature exhaust discharged from various engines of different systems that use the fuel gas separated by the gas-liquid separator 43, and the heat exchanger 41 (low-temperature channel 46). Heat exchange with steam generated in As a result, the steam absorbs heat from the above-described high-temperature discharge and is heated, and after the high-temperature discharge is cooled, it is discharged as exhaust gas.

The heat exchanger 52 sends the steam heated by exchanging heat between the steam heated by the heat exchanger 51 and the exhaust gas of the gasification reactor 31 to various engines using the steam of another system described above. .
The heat exchanger 53 heats the air sent from the combustion air fan 32 using the exhaust gas of the gasification reactor 31 sent via the heat exchanger 50. By these steps, the exhaust gas discharged from the gasification reactor 31 is discharged in a cooled state.

  At this time, for example, a part of the gas (product gas) separated by the gas-liquid separator 43 is a gasification reactor as in the gasification system 10 shown in FIG. 31 may be supplied and consumed as fuel gas.

  In the second embodiment, the slurry sent from the raw material preparation unit 20 to the gasification reactor 31 is used in the heat exchanger 50 using the exhaust gas from the gasification reactor 31 introduced through the heat exchanger 52. Therefore, the gasification process in the gasification reactor 31 can be made more efficient.

  Next, a third embodiment will be described with reference to FIG. 6 in which the same reference numerals are assigned to corresponding parts as in FIG. As shown in the figure, the gasification system 10 according to the third embodiment uses, for example, shochu residue as biomass, and a supply pump 23 is provided between the crusher 22 and the gasification reactor introduction pump 24. Except for the point provided and the point where the gas tank 47 and the dryer 60 are provided, the gasification system 10 of 1st Embodiment mentioned above is comprised substantially the same. Therefore, here, for the sake of convenience, different parts will be described, and detailed description of other overlapping parts will be omitted.

  Specifically, in the gasification system 10 of the present embodiment, the supply pump 23 supplies the slurry body discharged from the crusher 22 to the gasification reactor introduction pump 24. The gasification reactor introduction pump 24 pressurizes the slurry sent from the supply pump 23 and supplies it to the gasification reactor 31 of the heat treatment unit 30. The slurry body is pressurized to about 0.1 to 4 MPa by the gasification reactor introduction pump 24.

  The gas (product gas such as hydrogen or methane) separated by the gas-liquid separator 43 is sent to the gas tank 47. The gas tank 47 is a container for storing the gas (product gas) separated by the gas-liquid separator 43. Part of the product gas stored in the gas tank 47 is supplied to the gasification reactor 31 and consumed as fuel gas. In addition, this fuel gas can also be used as power generation or a power source.

  The combustion device 31a of the gasification reactor 31 introduces the combustion gas sent from the gas tank 47 into the liquefied petroleum gas (LPG) or the air from the combustion air fan 32 and burns it, and hydrothermally heats the slurry body. .

  Furthermore, in the present embodiment, a part of the shochu residue supplied to the adjustment tank 21 is supplied to the dryer 60. The dryer 60 is a waste steam generated by the low-temperature channel 46 of the heat exchanger 41, a residual drain heat of the liquid containing activated carbon and ash separated by the gas-liquid separator 43, and an exhaust heat of the gasification reactor 31 ( By using hot air), the shochu residue is dried to produce dry feed.

  At this time, for example, as in the gasification system 10 shown in FIG. 7 in which the same reference numerals are assigned to corresponding parts as in FIG. 6, a cooling tank 48 in which pure water is stored is used instead of the heat exchanger 41. Also good. In this cooling tank 48, pure water supplied by the water supply pump 44 is stored, and the treated fluid flowing through the high-temperature channel 45 is heat-exchanged with the pure water stored in the cooling tank 48, and the steam for power is supplied. Generated. The power steam is sent to the dryer 60 through the low temperature channel 46. As described above, the cooling tank 48 functions as a cooling mechanism that cools the treated fluid with pure water in the same manner as the heat exchanger 41.

  Further, for example, a centrifugal pump 25 that centrifuges and filters a part of the shochu residue may be provided as in the gasification system 10 shown in FIG. . The centrifugal pump 25 supplies the shochu residue, which has been dehydrated by centrifugation, to the dryer 60, and also filters the liquid phase of the shochu residue extracted by centrifugation and supplies it to the adjustment tank 21.

  At this time, as in the gasification system 10 shown in FIG. 9 in which the same reference numerals are assigned to corresponding parts to FIG. 8, a cooling tank 48 in which pure water is stored is used instead of the heat exchanger 41. Also good.

  In the third embodiment, a part of the shochu residue supplied to the adjustment tank 21 is supplied to the dryer 60, and the dry steam generated by the low-temperature channel 46 of the heat exchanger 41 and the gas-liquid separator 43 are used. Dry feed is produced by drying using the wastewater residual heat of the liquid containing the separated activated carbon and ash and the exhaust heat (hot air) of the gasification reactor 31. In this structure, it can utilize effectively as a dry feed produced | generated by drying a part of shochu residue with the dryer 60. FIG.

  It should be noted that the present invention can be appropriately changed without departing from the spirit or idea of the invention which can be read from the claims and the entire specification, and a supercritical water gasification system with such a change is also applicable to the present invention. It is included in the technical idea. For example, you may comprise as follows.

  For example, the raw material of biomass may be other than shochu residue, for example, egg-collecting chicken manure, sewage sludge and other water-containing biomass.

  In each of the above embodiments, water and a catalyst are mixed when the slurry body is generated, but these may not be mixed.

  DESCRIPTION OF SYMBOLS 2 ... Gasification system, 3 ... Heat exchanger, 4 ... Heater, 5 ... Gasification reactor, 6 ... Double pipe, 7 ... Inner piping, 8 ... Low temperature flow path, 9 ... Outer piping, 10 ... Gasification system, 11 ... high temperature flow path, 12 ... inlet, 13 ... slurry body, 14 ... high temperature fluid, 15 ... discharge port, 16 ... intermediate part, 17 ... low temperature part, 18 ... high temperature part, 20 ... raw material preparation part , 21 ... adjustment tank, 22 ... crusher, 23 ... supply pump, 24 ... gasification reactor introduction pump, 25 ... centrifugal pump, 30 ... heat treatment section, 31 ... gasification reactor, 31a ... combustion apparatus, 32 ... combustion Air fan, 40 ... gas processing unit, 41 ... heat exchanger, 41 ... pressure reducing mechanism, 42 ... cooling mechanism, 43 ... gas-liquid separator, 44 ... feed pump, 45 ... high temperature channel, 46 ... low temperature channel, 47: Gas tank, 48: Cooling tank. 50, 51, 52, 53 ... heat exchanger, 60 ... dryer

Claims (6)

A gasification system for generating fuel gas by decomposing a slurry body produced by preparing biomass in a supercritical state,
A raw material preparation unit for preparing the slurry body from the biomass;
A heat treatment part for heating and gasifying the slurry body prepared in the raw material preparation part;
A gas processing unit for extracting fuel gas from a supercritical high-temperature fluid sent from the heat treatment unit,
The heat treatment section includes a gasification reactor that generates the supercritical high-temperature fluid by heating and gasifying the slurry body,
A part or all of the high-temperature fluid is used as a heat source for heating other than direct heating of the slurry body ,
The biomass comprises a shochu residue, further comprising a dryer for drying the shochu residue,
The supercritical water gasification system , wherein the dryer dries the shochu residue using exhaust heat generated when the high-temperature fluid is generated in the gasification reactor . The gas processing unit has a heat exchanger in which the supercritical high-temperature fluid is introduced and heat-exchanges the high-temperature fluid and pure water.
In the gasification reactor, the slurry body sent from the raw material preparation unit is heated to a gasification reaction temperature at which gasification is possible, and the organic matter contained in the slurry body is hydrothermally treated,
The heat exchanger heat-exchanges the high-temperature fluid generated by the gasification reactor and pure water to heat the pure water to generate steam, and cools the high-temperature fluid. The supercritical water gasification system according to claim 1. The supercritical water gasification system according to claim 2 , wherein the heat exchanger comprises a cooling tank in which pure water is stored. The gas processing unit
The superheater according to claim 2 or 3 , further comprising a heat exchanger for exchanging heat of the steam with an exhaust from another heat engine that uses the product gas as fuel, and exhausting the steam as exhaust gas. Critical water gasification system. The heat treatment section further includes a heat exchanger that preheats the slurry body prepared in the raw material preparation section using exhaust heat of the gasification reactor. The supercritical water gasification system according to one item. The gasification reactor is
The supercritical water gasification system according to any one of claims 1 to 5, wherein a product gas extracted from a product generated by the gasification treatment is used as a fuel.