WO2020217399A1 - Système de gazéification d'eau supercritique - Google Patents

Système de gazéification d'eau supercritique Download PDF

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Publication number
WO2020217399A1
WO2020217399A1 PCT/JP2019/017696 JP2019017696W WO2020217399A1 WO 2020217399 A1 WO2020217399 A1 WO 2020217399A1 JP 2019017696 W JP2019017696 W JP 2019017696W WO 2020217399 A1 WO2020217399 A1 WO 2020217399A1
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Prior art keywords
heat exchanger
steam
water
gasification
type boiler
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PCT/JP2019/017696
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English (en)
Japanese (ja)
Inventor
泰孝 和田
博昭 谷川
幸彦 松村
良文 川井
琢史 野口
Original Assignee
中国電力株式会社
国立大学法人広島大学
中電プラント株式会社
株式会社東洋高圧
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Application filed by 中国電力株式会社, 国立大学法人広島大学, 中電プラント株式会社, 株式会社東洋高圧 filed Critical 中国電力株式会社
Priority to JP2019554705A priority Critical patent/JP6671677B1/ja
Priority to PCT/JP2019/017696 priority patent/WO2020217399A1/fr
Publication of WO2020217399A1 publication Critical patent/WO2020217399A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids

Definitions

  • the present invention relates to a supercritical water gasification system that produces fuel gas by decomposing a slurry body prepared by adding water and a catalyst to biomass in a supercritical state.
  • a general biomass gasification system is configured to include a heat exchanger, a heater, a gasification reactor, etc., and organic matter is converted into hydrogen, methane, ethane, carbon monoxide, carbon dioxide, etc. by hydrolysis.
  • Gasify is a device that heats a slurry body prepared by adding water and activated carbon (gasification catalyst) to biomass such as shochu residue, egg-collecting chicken manure, and sewage sludge and mixing them.
  • the heater is a device that raises the temperature of the slurry heated by the heat exchanger to 600 ° C., which is the gasification reaction temperature.
  • the gasification reactor is a device that hydrothermally heats the slurry to gasify organic substances into a supercritical high-temperature fluid.
  • the fluid in the supercritical state is then heat-exchanged to room temperature and gas-liquid separated, and the gas is used as fuel gas.
  • fine powder of a non-metal catalyst for example, activated carbon
  • inorganic substances derived from raw materials and tar produced during gasification.
  • Char, etc. may cause obstruction in the double tube of the double tube heat exchanger or between the inner tube and the outer tube.
  • the treated fluid after the gasification reaction flows between the inner tube and the outer tube of the double-tube heat exchanger having a total length of about 100 m, and by heat exchange with the slurry body flowing in the inner tube. After the liquid temperature is lowered, it is further cooled and separated into gas and liquid to separate into gas and wastewater. Then, the gas is used as fuel, and the surplus gas is accumulated in the tank and used separately. At this time, in such a double-tube heat exchanger, the heat of the treated fluid is used for heating the slurry body which is a gasification raw material.
  • tar and char generated from the slurry body flowing in the inner pipe of the double-tube heat exchanger may cause blockage in the heat exchanger inner pipe and the pipes after its outlet, which in turn may cause the system to stop. was there.
  • heat exchangers are expensive because they can withstand high temperatures and pressures and are welded by engineers who have cleared legal regulations using thick piping made of expensive materials. Therefore, there is a demand to raise the temperature efficiently by using a heat exchanger as small as possible. For example, in the case of a heat exchanger having a long overall length, it takes time to raise the temperature. Since tar and char are generated in the medium and high temperature parts, if the reaction time here is long, the amount of tar and char generated increases, which may lead to blockage of the flow path at the inner pipe outlet of the heat exchanger. was there.
  • the present inventors have set the slurry body at a temperature close to the gasification reaction temperature and the pressure of the supercritical water gasification system. We focused on preheating using steam with a pressure close to.
  • the present invention has been made in view of the above problems, and the heat exchanger is made compact while minimizing the fuel cost, the generation of tar and char is suppressed, and the pipe blockage of the heat exchanger is avoided. It is an object of the present invention to provide a supercritical water gasification system capable of more efficiently producing fuel gas such as methane, hydrogen and carbon monoxide from water-containing biomass.
  • the supercritical water gasification system is used.
  • a gasification reactor that prepares biomass and gasifies the produced slurry body into supercritical water gasification, and a first heat exchange that preheats the slurry body before it is subjected to supercritical water gasification treatment by the gasification reactor.
  • a supercritical water gasification system that is equipped with a vessel and decomposes the slurry in a supercritical state to generate fuel gas.
  • a heating unit having a drum-type boiler that discharges steam used for preheating the slurry in the first heat exchanger.
  • a flow rate adjusting unit provided in a flow path connecting the heating unit and the first heat exchanger to control the flow rate of the steam is provided. The flow rate adjusting unit is characterized in that the temperature of the slurry body at the outlet of the first heat exchanger is controlled by adjusting the flow rate of the steam.
  • the supercritical water gasification system is A second heat exchanger different from the first heat exchanger is further provided.
  • the first heat exchanger may cool the product of the gasification reactor by utilizing the steam whose temperature has dropped by preheating the slurry body in the first heat exchanger.
  • the heating unit further includes a water supply pump for supplying water to the drum type boiler and a drive turbine for driving the water supply pump.
  • the drive turbine may be driven by using steam after cooling the product in the second heat exchanger.
  • the heating unit may further include a circulation flow path for circulating water between the drum type boiler and the water supply flow path to the drum type boiler.
  • the drum type boiler may use the generated gas generated by the gasification treatment as fuel.
  • preheating in the heat exchanger is preferably performed with steam at 538 ° C. to 566 ° C. in the vicinity when the reactor temperature is 600 ° C.
  • the slurry body is preheated by using the steam from the heating part in the heat exchanger to make the heat exchanger compact while minimizing the fuel cost, and the temperature rise rate can be increased by making the compact.
  • FIG. 1 is a diagram showing a schematic configuration of a supercritical water gasification system described as an embodiment of the present invention.
  • the supercritical water gasification system according to the present invention (hereinafter, may be simply referred to as “system” as appropriate) includes a adjusting tank 100, a crusher 110, a supply pump 120, and a first heat.
  • the drum type boiler 140, the first heat exchanger 130, and the second heat exchanger 131 are connected by the flow path 150.
  • a flow path 150 includes a flow rate adjusting valve 160 between the drum type boiler 140 and the first heat exchanger 130. Then, the steam (details will be described later) sent from the drum type boiler 140 is circulated between the drum type boiler 140 / first heat exchanger 130 and the second heat exchanger 131 and used for each purpose. ing.
  • the configuration of the flow path 150 is an example and is not limited to this.
  • the first heat exchanger 130 (a heat exchanger that preheats the slurry body before being gasified by supercritical water in the gasification reactor 141) and the second heat exchanger 131 (slurry).
  • the third heat exchanger 132 (second heat from the gasification reactor 141)
  • a fourth heat exchanger 133 (using water supplied from the condensate pump 193).
  • each of the heat exchangers (heat exchangers that cool the product sent from the three heat exchangers 132 to almost room temperature and recover heat) is composed of double-tube heat exchangers, but the present invention describes this. Not exclusively.
  • the adjustment tank 100 is a tank that mixes water-containing biomass (may be a slurry of biomass. The same applies hereinafter), a non-metallic catalyst, water, and the like.
  • the slurry body processed by this system is a mixture of the hydrous biomass and the non-metal catalyst charged into the adjusting tank 100 and the water charged as needed, and the non-metal catalyst is suspended on the hydrous biomass. Prepared by turbidity. It should be noted that the addition of water is appropriately performed according to the water content of the biomass.
  • the water-containing biomass is, for example, shochu residue, egg-collecting chicken manure, sewage sludge, or the like.
  • non-metal catalyst for example, activated carbon, zeolite, a mixture thereof and the like can be used, but it is preferable to use a powder having an average particle size of 200 ⁇ m or less, and porous particles having an average particle size of 200 ⁇ m or less. Is more preferable to use.
  • the crusher 110 crushes the biomass in the slurry prepared in the adjustment tank 100 to make the biomass a uniform size in advance (preferably, the average particle size is 800 ⁇ m or less, more preferably the average particle size is 300 ⁇ m or less). It is a device for.
  • the drum type boiler 140 as a heating unit includes a water cooling wall 143, a superheater 144, and a drum 145, and water-cools the water supplied from the water supply pump 180 and preheated via the third heat exchanger 132. It is heated by the wall 143 to generate steam, which is further overheated by the superheater 144 fed through the drum 145. Then, steam of about 538 ° C. to 566 ° C. and about 15 MPa to 20 MPa generated by such overheating is supplied to the first heat exchanger 130. At this time, the water supply pump 180 is driven by a drive turbine 181 that utilizes steam (steam after cooling the product produced by the gasification reactor 141) supplied from the second heat exchanger 131 described later. To.
  • the drum type boiler 140 can use inexpensive fuel such as coal and heavy oil, and can generate steam with high boiler efficiency, so that steam can be supplied at low cost.
  • the gasification reactor 141 is prepared by adding water or a non-metallic catalyst to water-containing biomass in the adjustment tank 100 to prepare a slurry, or adding a non-metallic catalyst to the biomass crushed by the crusher 110 and mixing them.
  • This is an apparatus for gasifying the biomass in the slurry by supercritical water gasification treatment of the prepared slurry.
  • the condition is preferably a supercritical state (that is, a condition of 374 ° C. or higher and 22.1 MPa or higher), but under a temperature and pressure (600) that can suppress the formation of tar and char and increase the carbon gasification rate. ° C. or higher, in the range of 25 to 35 MPa) is more preferable.
  • fuel gas such as methane, hydrogen gas, carbon monoxide, ethane, and ethylene.
  • the gasification reactor 141 includes a temperature measuring device for measuring the internal fluid temperature and the external combustion gas temperature thereof, and a pressure measuring device for measuring the internal fluid pressure and the inlet / outlet differential pressure of the gasification reactor 141. Both are not shown), and it is preferable to provide.
  • the gasification reactor 141 is provided with a reactor burner 142, and a coiled pipe (not shown) is heated by the reactor burner 142.
  • a tubular reactor When such a tubular reactor is used, there is an advantage that the reaction time can be secured for a certain period of time by adjusting the diameter and length of the pipe.
  • the gasification reactor is not limited to this, and a catalyst layer reactor, a fluidized bed reactor, a jet bed reactor, and the like can be widely applied.
  • the apparatus is not particularly limited as long as it is an apparatus capable of hydrothermally treating a slurry containing biomass under the above-mentioned conditions.
  • the first heat exchanger 130 which is configured as a double-tube heat exchanger, heats the steam supplied from the drum type boiler 140 (in this case, steam of about 538 ° C. to 566 ° C. and steam of about 15 MPa to 20 MPa). It is a device that preheats a slurry in which a non-metallic catalyst is suspended in water-containing biomass to be supercritically hydrogasified by a gasification reactor 141 to a predetermined temperature (in this case, around 600 ° C.). ..
  • the temperature difference becomes small in the intermediate portion due to the physical properties of water. That is, since the slurry body pressure is higher than the treated fluid pressure, the pseudo-critical point temperature is higher in the slurry body than in the treated fluid, and the constant pressure specific heat of water is maximum at the pseudo-critical point.
  • the temperature difference between the treated fluid and the slurry body becomes small in a large range. Therefore, the amount of heat exchanged per unit heat transfer area is reduced, and there is a risk that heat exchange becomes inefficient.
  • the large change in density near the pseudo-critical point temperature is also a cause of the small temperature difference.
  • the total length is formed to increase the amount of heat exchanged, so it takes time to raise the temperature.
  • Tar and char are generated in the medium and high temperature parts, but if it takes time to raise the temperature, the tar and char generation time here will increase, and the amount of tar and char generated will increase, which in turn will increase the inside of the heat exchanger and its outlet. There was a risk that the piping would be blocked.
  • the first heat exchanger 130 uses the steam supplied from the drum type boiler 140 (in this case, steam of about 538 ° C. to 566 ° C. and steam of about 15 MPa to 20 MPa) to form the above slurry. I tried to preheat. That is, the first heat exchanger 130 can preheat the slurry body supplied to the gasification reactor 141 so as to approach 600 ° C. before being gasified by supercritical water in the gasification reactor 141. ..
  • the double pipe in the first heat exchanger 130 is composed of an outer pipe and an inner pipe like the existing double pipe heat exchanger, and is provided by the supply pump 120.
  • the supplied slurry body flows through the flow path in the inner pipe, and the steam supplied from the drum type boiler 140 flows through the flow path between the outer pipe and the inner pipe. That is, in the first heat exchanger 130, the slurry body flows in the flow path in the inner pipe and is supplied to the gasification reactor 141, and the direction in which the slurry body flows with respect to the flow path between the outer pipe and the inner pipe. Steam flows in the opposite direction and is supplied to the second heat exchanger 131.
  • a flow rate adjusting valve 160 as a flow rate adjusting unit for controlling the flow rate of steam supplied from the drum type boiler 140 is provided in the flow path 150 connecting the drum type boiler 140 and the first heat exchanger 130. ing.
  • the flow rate adjusting valve 160 controls the flow rate of steam (steam for preheating the slurry body) supplied from the drum type boiler 140 to control the steam (about 538 ° C. to 566 ° C. and about 15 MPa to 20 MPa).
  • the temperature of the steam (in other words, the preheating temperature of the slurry body) is maintained at around 600 ° C. (preferably about 538 ° C. to 566 ° C.).
  • thermometer (not shown) on the outlet side of the pipe through which the slurry body from the supply pump 120 in the first heat exchanger 130 flows to adjust the flow rate adjusting valve 160.
  • the flow rate adjusting valve 160 may maintain the steam at about 15 MPa to 20 MPa by controlling the flow rate of the steam supplied from the drum type boiler 140. In this case, maintaining the steam pressure is prioritized over the preheating temperature of the slurry.
  • the first heat exchanger 130 can be significantly made compact by preheating the slurry body using the steam supplied from the drum type boiler 140.
  • the generation of tar and char is suppressed to avoid blockage of the piping of the first heat exchanger 130, and fuel gas such as methane, hydrogen, and carbon monoxide from the water-containing biomass.
  • fuel gas such as methane, hydrogen, and carbon monoxide from the water-containing biomass.
  • the steam is sent to the second heat exchanger 131, the drive turbine 181 for driving the water supply pump 180, the steam turbine 190, etc., which will be described later, via the flow path 150, and is reused for each purpose. , The fuel consumption of the whole system can be minimized.
  • the second heat exchanger 131 which functions as a cooler, is a device for cooling and recovering heat of the discharge discharged from the gasification reactor 141 via the first heat exchanger 130.
  • the steam after preheating the slurry body discharged from the first heat exchanger 130 and the above-mentioned discharge (product produced by the gasification reactor 141) are heat-exchanged.
  • the discharge is cooled from 600 ° C. to 150 ° C. to 200 ° C. and heat is recovered for effective use.
  • the third heat exchanger 132 which functions as a cooler like the second heat exchanger 131, cools the discharge supplied from the second heat exchanger 131 and recovers the heat to the thermal power generation system side. It is a device of.
  • the discharge is cooled from 150 ° C. to 200 ° C. to 100 ° C. to 150 ° C. by exchanging heat between the water supplied from the water supply pump 180 and the discharge.
  • the fourth heat exchanger 133 exchanges heat between the water supplied from the condensate pump 193 and the discharge, thereby cooling the discharge from 100 ° C. to 150 ° C. to almost room temperature.
  • the water after cooling the discharge is supplied to the water cooling wall 143 via the deaerator 200 / water supply pump 180 and the third heat exchanger 132, and then heated to the superheater 144 in the state of steam. Will be sent to.
  • the depressurizer 134 is arranged between the fourth heat exchanger 133 and the gas-liquid separator 170, and is arranged from the gasification reactor 141 to the second heat exchanger 131, the third heat exchanger 132, and the fourth heat exchanger.
  • the discharge discharged via 133 is depressurized from 25 MPa to a pressure at which gas can be sent to the place of consumption and pressure can be stored in the container.
  • the emissions discharged from the gasification reactor 141 contain highly flammable fuel gas (for example, methane, hydrogen, carbon monoxide, ethane, ethylene), water vapor, etc., so the pressure is reduced.
  • the device 134 cools and depressurizes the exhaust gas, thereby reducing the risk of fire and the like, and converting water vapor into water to facilitate gas-liquid separation.
  • the second heat exchanger 131, the third heat exchanger 132, and the fourth heat exchanger 133 are taken as examples as devices for cooling and recovering heat of the discharge discharged from the gasification reactor 141.
  • the cooler is not limited to these, and any device may be used as long as it can cool the discharge discharged from the gasification reactor 141.
  • the decompressor is not limited to the decompression device 134.
  • the heat exchanger described above is not limited to the countercurrent type, and may be, for example, a parallel flow type. Further, the heat exchanger is not limited to the double tube type heat exchanger, and for example, a spiral type or plate type heat exchanger may be used.
  • this system equipped with at least the first heat exchanger 130 (further when the second heat exchanger 131, the third heat exchanger 132 and the fourth heat exchanger 133 are included) is excellent in economy. ..
  • the gas-liquid separator 170 uses the discharges supplied through the gasification reactors 141 and the second to fourth heat exchangers 131 to 133 in sequence with the generated gas (gas component) including fuel gas and water or water. It is a device that separates ash and non-metallic catalyst into liquid components suspended in water.
  • the gas-liquid separator 170 an existing gas-liquid separator such as a separator can be used.
  • the gas tank 171 is a container (preferably a pressure-resistant container) for storing the gas component (produced gas) separated by the gas-liquid separator 170.
  • the discharge decompressed by the decompression device 134 and transferred to the gas-liquid separator 170 is a generated gas (gas component) containing fuel gas and a mixed solution (liquid component) of water, ash, non-metallic catalyst, etc.
  • the produced gas is stored in the gas tank 171.
  • the mixed solution contains a non-metal catalyst
  • the non-metal catalyst may be recovered by separating the ash, the non-metal catalyst, and water by the catalyst recovery device 172. This makes it possible to reuse the non-metal catalyst.
  • the superheater 144 arranged in the drum type boiler 140 is sent from the condensate pump 193 via the fourth heat exchanger 133, the deaerator 200, the water supply pump 180, and the third heat exchanger 132, and is sent by the water cooling wall 143.
  • Heat for further raising the temperature of the heated steam by using the heat of combustion in a part of the generated gas stored in the gas tank 171 or in a gas containing oxygen such as the atmosphere in a fuel gas (LNG, LPG, etc.). This is a group of replacement pipes.
  • the drum type boiler 140 is the above-mentioned steam heated by using a part of the generated gas stored in the gas tank 171 or the combustion heat in a gas containing oxygen such as the atmosphere in a fuel gas (LNG, LPG, etc.).
  • a gas containing oxygen such as the atmosphere in a fuel gas (LNG, LPG, etc.).
  • LNG, LPG, etc. a fuel gas
  • This is an apparatus that preheats a slurry in which a non-metallic catalyst is suspended in a water-containing biomass to a predetermined temperature (in this case, around 600 ° C.) by heating the first heat exchanger 130.
  • the fuel of the drum type boiler 140 is not limited to gas fuel, but may be solid fuel such as coal or woody biomass or liquid fuel such as heavy oil or light oil.
  • the generated gas may be used in combination.
  • the drum type boiler 140 heats the steam generated while circulating the water in the drum 145 between the flow path connecting the water cooling wall 143 and the drum 145 and the
  • the supply pump 120 is a device that supplies the slurry body prepared in the adjusting tank 100 or the slurry body obtained by crushing the biomass with the crusher 110 to the first heat exchanger 130.
  • the slurry body is supplied to the gasification reactor 141 via the first heat exchanger 130 (the flow path in the inner pipe of the double pipe).
  • a plunger pump, a high-pressure piston pump, a diaphragm pump, or the like can be used.
  • the steam turbine 190 is arranged in, for example, a thermal power plant (not shown) and is connected to this system (specifically, a superheater 144 in a drum type boiler 140) via a heat transfer tube. Then, by utilizing the steam of the drum type boiler 140 and the steam discharged from the second heat exchanger 131, the steam turbine 190 is rotated to generate electricity with the generator 191 connected coaxially, and then the steam is generated. The water is restored by the condenser 192.
  • the system may be provided with a power generation device that generates electricity by using the generated gas stored in the gas tank 171 as fuel.
  • the power generation device can be widely applied to existing devices such as a gas engine, a gas turbine, a Stirling engine, and a fuel cell.
  • biomass that is, aggregates of polymers can be decomposed individually, so that the fluidity is increased and the biomass is treated by the gasification reactor 141. It is possible to improve the contact efficiency between biomass and water or non-metallic catalysts, further suppress the formation of tar and char, and efficiently generate fuel gas such as methane, hydrogen, and carbon monoxide from biomass. ..
  • the generated gas containing the fuel gas can be generated from the emissions discharged from the gasification reactor 141. Can be safely collected.
  • the biomass can be crushed in advance, so that the efficiency of slurry and gasification of biomass can be improved.
  • the heat of the steam discharged from the drum type boiler 140 is used to preheat the slurry body transferred to the gasification reactor 141 by the first heat exchanger 130 to preheat the gas. Since the slurry body can be reliably transferred to the chemical reactor 141 in a state near the steam temperature sent from the drum type boiler 140, it is possible to avoid a state such as insufficient temperature rise of the slurry body. Therefore, the heater provided between the first heat exchanger 130 and the gasification reactor 141 in the conventional system can be eliminated.
  • this system preheats the gasification reactor 141 for supercritical water gasification treatment of the slurry containing the aqueous biomass and the slurry before being treated with the gasification reactor 141.
  • It includes a first heat exchanger 130, a drum-type boiler 140 as a heating unit, and a flow rate adjusting valve 160 for controlling the flow rate of steam.
  • the flow rate adjusting valve 160 is arranged in the flow path 150 that connects the first heat exchanger 130 and the drum type boiler 140.
  • the first heat exchanger 130 uses the steam of the drum type boiler 140 (in this case, the main steam of about 538 ° C. to 566 ° C. and about 15 MPa to 20 MPa) for heating the slurry body flowing through the inner pipe.
  • the drum-type boiler 140 as a heating unit is not limited to the above-described embodiment, and includes, for example, a gasification reactor 141, and the gasification reactor 141 is provided by utilizing the combustion of the drum-type boiler 140. It may be heated. In this case, it is not necessary to separately provide a heating means (for example, a reactor burner 142) for heating the gasification reactor 141, and the configuration of the entire system can be simplified.
  • a heating means for example, a reactor burner 142
  • the drum type boiler 140 as a heating unit may heat the gasification reactor 141 by utilizing the heat of the above-mentioned steam discharged from the drum type boiler 140.
  • a coil-shaped heating pipe or the like to which steam is supplied from the drum type boiler 140 is provided outside (outer peripheral surface) or inside of the coil (not shown) of the gasification reactor 141. It is preferable to arrange it on the (inner peripheral surface) to form a double pipe. In this case, since the steam discharged from the drum type boiler 140 can be effectively used as a heat source, the slurry body can be efficiently heated by the gasification reactor 141.
  • the drive source of the steam turbine 190 is not limited to the steam discharged from the drum type boiler 140.
  • the steam or the like supplied sequentially via the first heat exchanger 130 and the second heat exchanger 131 is used.
  • the steam turbine 190 may be driven.
  • the mass ratio of the non-metal catalyst and the biomass (dry biomass) when preparing a mixture of biomass, non-metal catalyst and water in the adjustment tank 100 is in the range of 1: 1 to 20.
  • the amount of water to be mixed is preferably adjusted so that the water content of the biomass is 70 to 99 wt%. As a result, the gasification rate of biomass can be increased.
  • the hydrothermal treatment conditions for the biomass slurry in the gasification reactor 141 are not particularly limited as long as they are supercritical water conditions (374 ° C. or higher and 22.1 MPa or higher), but they suppress the formation of tar and char. It is preferable to carry out under a temperature (500 ° C. or higher) and a pressure (range of 25 to 35 MPa) at which the gasification rate can be increased, and from the viewpoint of gasification rate, equipment cost and deterioration prevention, the conditions of 600 ° C. and 25 MPa are set. Especially preferable.
  • the generated gas stored in the gas tank 171 is supplied to the drum type boiler 140 / reactor burner 142 and burned.
  • the drum type boiler 140 / reactor burner 142 burns the supplied generated gas as fuel in a gas containing oxygen such as the atmosphere, and gasifies the steam of the water cooling wall 143 and / or the superheater 144 or gasification.
  • the slurry inside the reactor 141 is heated.
  • combustion gas of the drum type boiler 140 may be supplied to the gasification reactor 141 to heat the slurry body.
  • the steam supplied to the second heat exchanger 131 absorbs heat from the product generated in the gasification reactor 141, thereby causing the said steam.
  • the product is cooled, it is transferred to the drive turbine 181 and the steam turbine 190, and is used for driving the drive turbine 181 and the steam turbine 190.
  • the high-temperature and high-pressure steam after cooling the product discharged from the second heat exchanger 131 is used for the drive turbine 181 for driving the feed water pump 180 and the steam turbine 190 (second stage and subsequent stages). ), But it can be widely applied to steam utilization destinations where pressure and temperature conditions such as feed water heaters, deaerators, and small turbines are appropriate.
  • the supercritical water gasification system is not limited to the above-described embodiment, and for example, as shown in FIG. 2 in which the corresponding portions corresponding to those in FIG. 1 are designated by the same reference numerals, the second heat exchanger 131 (see FIG. 1). ) Is not provided, and the steam after preheating the slurry body discharged from the first heat exchanger 130 is lower than the temperature of the flow path 150 downstream of the first heat exchanger 130 and the pressure of the flow path 150. It may be collected in a lower place (for example, the deaerator 200). In addition, as the collection point, an outlet of the condensate pump 193, a feed water heater (not shown), and the like can also be applied. Further, the recovery location may be switched depending on the temperature and pressure conditions in the flow path 150 downstream of the first heat exchanger 130.
  • non-metal catalyst used in the present embodiment examples include activated carbon, zeolite, and a mixture thereof. Further, as the catalyst, a metal-based catalyst or an alkaline catalyst can be used.

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Abstract

Dans la présente invention, un premier échangeur de chaleur (130) préchauffe un corps de bouillie comprenant une biomasse contenant de l'eau en utilisant de la vapeur provenant d'une chaudière de type tambour (140), ce qui permet de réduire au minimum le coût de carburant, de réduire la taille du premier échangeur de chaleur (130), de supprimer la génération de goudron et de résidus de carbonisation, d'empêcher la tuyauterie du premier échangeur de chaleur (130) de s'obstruer, et de générer de manière plus efficace un gaz combustible. En outre, lorsqu'un préchauffage est effectué, une soupape de régulation de débit (160) régule le débit de la vapeur pour contrôler la température du corps de bouillie à la sortie du premier échangeur de chaleur (130), ce qui permet d'éviter une augmentation insuffisante de la température de celui-ci à la sortie du premier échangeur de chaleur (130). Par conséquent, la présente invention peut éliminer l'élément chauffant disposé entre le premier échangeur de chaleur (130) et un réacteur de gazéification (141) dans le système classique.
PCT/JP2019/017696 2019-04-25 2019-04-25 Système de gazéification d'eau supercritique WO2020217399A1 (fr)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002263465A (ja) * 2001-03-07 2002-09-17 Saka Shiro 超臨界水又は亜臨界水による有機物質等の反応装置
WO2016135979A1 (fr) * 2015-02-27 2016-09-01 中国電力株式会社 Système de gazéification d'eau supercritique et procédé de gazéification
WO2016139723A1 (fr) * 2015-03-02 2016-09-09 中国電力株式会社 Système de gazéification
WO2018083785A1 (fr) * 2016-11-04 2018-05-11 中国電力株式会社 Système de gazéification à eau supercritique

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002263465A (ja) * 2001-03-07 2002-09-17 Saka Shiro 超臨界水又は亜臨界水による有機物質等の反応装置
WO2016135979A1 (fr) * 2015-02-27 2016-09-01 中国電力株式会社 Système de gazéification d'eau supercritique et procédé de gazéification
WO2016139723A1 (fr) * 2015-03-02 2016-09-09 中国電力株式会社 Système de gazéification
WO2018083785A1 (fr) * 2016-11-04 2018-05-11 中国電力株式会社 Système de gazéification à eau supercritique

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