WO2011129302A1 - Coal gasification furnace - Google Patents
Coal gasification furnace Download PDFInfo
- Publication number
- WO2011129302A1 WO2011129302A1 PCT/JP2011/059020 JP2011059020W WO2011129302A1 WO 2011129302 A1 WO2011129302 A1 WO 2011129302A1 JP 2011059020 W JP2011059020 W JP 2011059020W WO 2011129302 A1 WO2011129302 A1 WO 2011129302A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- coal
- reaction vessel
- burner
- partial oxidation
- gasification furnace
- Prior art date
Links
Images
Classifications
-
- 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
- C10J3/723—Controlling or regulating the gasification process
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/466—Entrained flow processes
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
- C10J3/487—Swirling or cyclonic gasifiers
-
- 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
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
-
- 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
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1678—Integration of gasification processes with another plant or parts within the plant with air separation
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
-
- 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
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1846—Partial oxidation, i.e. injection of air or oxygen only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
Definitions
- the present invention relates to a coal gasification furnace that produces combustible gas by gasifying coal with an oxidizing agent such as oxygen gas or water vapor.
- Patent Document 1 Conventionally, as a gasification furnace (coal gasification furnace) for producing a combustible gas from pulverized coal or the like, for example, the one shown in Patent Document 1 is known.
- this gasification furnace four combustor burners are arranged at equal distances on a circumference in a predetermined plane in a pressure vessel (reaction vessel) in a plan view.
- the two sets of combustor burners arranged at symmetrical positions across the central axis of the circumference are arranged so as to face each other.
- the combustor burner consists of a light oil burner for gasifier start-up provided in the center, and an air nozzle, char nozzle, fuel coal nozzle, and secondary air nozzle arranged concentrically with the light oil burner from the inside to the outside. It is configured. Air, char (ungasified coal residue or pyrolysis residue), and fuel coal are swung in their respective nozzles, then ignited by a light oil burner and injected into a pressure vessel.
- gas generated by gasification rises in the gasification furnace, but if the flow of gas in the gasification furnace rises unevenly, carbon (char) in the coal is sufficiently gasified. Before it reacts, it may flow out of the gasifier and the reaction rate (conversion rate of carbon in coal to gas) may decrease.
- the present invention has been made in view of such problems, and can sufficiently react coal in a compact reaction vessel and can stably attach slag to the inner peripheral surface of the reaction vessel.
- the object is to provide a highly efficient coal gasifier.
- the coal gasifier of the present invention is A reaction vessel formed in a cylindrical shape extending upward and provided with a discharge port on the upper end side; A plurality of a plurality of flat plates are provided on a reference plane that is parallel to a horizontal plane and located below the discharge port and spaced circumferentially on the inner peripheral surface of the reaction vessel, and supplies coal and an oxidant into the reaction vessel.
- each of the burner parts has its own axis smaller than the inner diameter of the reaction vessel and is in contact with a virtual circle centered on the center axis in the same direction, and its own axis is parallel to the horizontal plane. Alternatively, it is arranged so as to be directed downward toward the tip of the burner portion.
- a coal gasification furnace that produces at least hydrogen gas and carbon monoxide gas by gasifying coal in a reaction vessel, A reaction vessel formed in a cylindrical shape extending upward; An outlet provided on the upper end side of the reaction vessel; A plurality of cylindrical burner portions for supplying coal and oxidant into the reaction vessel; The plurality of burner portions are provided on a reference plane parallel to a horizontal plane located below the discharge port, with an interval in the circumferential direction of the inner peripheral surface of the reaction vessel, When viewed from above the reaction vessel, each burner portion has an axis line in contact with a virtual circle having a diameter smaller than the inner diameter of the reaction vessel centered on the central axis line of the reaction vessel, in the same direction. Place the part, The burner portion is arranged such that an axis of the burner portion is parallel to a horizontal plane or is directed downward toward the tip of the burner portion.
- the burner part is arrange
- the coal is expanded by gasification, and the coal that is going to rise while swirling in the reaction vessel is made to flow horizontally or downward once from the burner section, thereby increasing the time for the coal to flow through the reaction vessel and from the discharge port.
- the gas can be sufficiently gasified in the reaction vessel before being discharged.
- the burner portions are arranged at regular intervals around the central axis of the reaction vessel. According to the present invention, the flow of fluid containing coal and oxidant supplied from the burner section and gas generated by combustion of coal in the reaction vessel can be further stabilized.
- the ratio of the diameter of the virtual circle to the inner diameter of the reaction vessel is more preferably set to 1/10 or more and 1/3 or less.
- the ratio of the diameter of the virtual circle to the inner diameter of the reaction vessel (hereinafter also referred to as “diameter ratio”) to 1/3 or less, the velocity gradient of the fluid on the inner peripheral surface of the reaction vessel can be obtained. It is made small and it is suppressed that the slag adhering to the internal peripheral surface of reaction container peels from an internal peripheral surface. Therefore, it is possible to prevent the inner peripheral surface of the reaction vessel from being exposed to a high temperature, thereby reducing the performance due to an increase in heat loss and damaging the inner peripheral surface.
- the diameter ratio to 1/10 or more, coal and oxidant supplied from the burner portion are prevented from colliding with each other from the front, and the flow swirling around the central axis of the reaction vessel is ensured. As a result, the gasification reaction time can be lengthened and the reaction rate can be improved.
- mass flow rates of the coal and the oxidant supplied from the burner portions into the reaction vessel are m1 (kg / s) and m2 (kg / s), respectively.
- the average flow rate Va (m / s) according to the equation (1) is 10 (m / S) and more preferably 50 (m / s) or less.
- Va (m1 ⁇ V1 + m2 ⁇ V2) / (m1 + m2) (1)
- the average flow velocity Va 50 (m / s) or less, it is possible to suppress the slag adhering to the inner peripheral surface of the reaction vessel from being peeled off from the inner peripheral surface and to be transmitted from the reaction vessel to the outside. Heat loss can be reduced.
- coal can be stably conveyed with an oxidizing agent in a burner part because average flow velocity Va shall be 10 (m / s) or more.
- the angle of the axis of each burner part with respect to the horizontal plane is more preferably set to 0 ° or more and 10 ° or less. According to the present invention, by setting the angle to 0 ° or more and 10 ° or less, the coal particles blown from the burner part can exist in the high-temperature field near the burner part for a long time. It is promoted and the reaction rate can be increased.
- a char burner is arranged in the same manner as the burner portion on the second reference plane parallel to the reference plane and immediately above the burner portion in the reaction vessel. More preferably.
- the char gasification reaction rate of carbon in coal is 99% or more by recycling the char recovered unreacted by the char burner of the reaction vessel to the coal gasification furnace to cause the gasification reaction. can do.
- coal can be sufficiently reacted in a compact reaction vessel, and slag can be stably adhered to the inner peripheral surface of the reaction vessel.
- FIG. 3 is a plan sectional view taken along a cutting line AA in FIG. 2. It is a figure which shows the flow-velocity distribution in the reference plane in FIG. It is a figure which shows the relationship between the heat loss ratio with respect to the diameter ratio in the partial oxidation part of the coal gasification furnace, and the reaction rate ratio. It is a figure which shows the relationship of the heat loss ratio with respect to the average flow velocity of coal and an oxidizing agent in the coal gasifier.
- a coal gasification furnace is an apparatus that is used by being incorporated in a part of a coal gasification system, and that produces at least hydrogen gas and carbon monoxide gas by burning coal inside.
- the coal gasification synthesis gas production system 1 is a plant facility that produces synthesis gas mainly composed of hydrogen gas and carbon monoxide gas using coal as a raw material. By supplying this product synthesis gas as a raw material for chemical synthesis equipment, methane, methanol, ammonia and the like can be finally produced.
- a coal gasification synthesis gas production system 1 includes a coal pulverization / drying facility 2, a coal supply facility 3, a coal gasification furnace 4 of the present embodiment, a heat recovery facility 5, a char recovery facility 6, and a shift reaction facility. 7, a gas purification facility 8, and an air separation facility 9.
- the outer diameter of coal is not uniform, and depending on the type, coal may contain more water than desired. Therefore, first, in the coal pulverization / drying facility 2, the coal is pulverized so as to become pulverized coal having an average particle size of about 30 to 60 ( ⁇ m) and about 75% of 200 mesh or less, and further has a predetermined moisture content, preferably Is dried so that the total water content is 10% or less, and then supplied to the coal supply facility 3. In addition, from the coal pulverization / drying facility 2 to the coal gasification furnace 4, the coal moves in a sealed space so that the moisture content in the dried coal does not change.
- the coal is pressurized to a predetermined pressure by a carrier gas or the like in the coal supply facility 3, and then a predetermined weight is supplied to the coal gasification furnace 4 by airflow conveyance. A fixed amount is supplied.
- the operating pressure of the coal gasification furnace is not particularly limited, but is preferably 2 MPaG or more and 5 MPaG or less from the viewpoint of improving reaction efficiency by reducing the gasification furnace, reducing facility costs, and utility costs.
- the air separation facility 9 compresses and liquefies air, and separates dried oxygen gas, nitrogen gas, and the like from the liquid air due to a difference in boiling point.
- the oxygen gas separated by the air separation facility 9 is supplied to the coal gasification furnace 4 at a predetermined flow rate.
- the coal gasification furnace 4 has at least a partial oxidation part (reaction vessel) 12 in an upper part D ⁇ b> 1, and a preheating part 15 is provided in a lower part D ⁇ b> 2 of the partial oxidation part 12.
- the partial oxidation unit 12 and the preheating unit 15 communicate with each other in the vertical direction D.
- the partial oxidation portion 12 is formed in a cylindrical shape extending in the vertical direction D with a heat-resistant refractory or the like, and on the inner peripheral surface of the partial oxidation portion 12 along the axis C ⁇ b> 1.
- Eight burner portions 17a to 17h formed in a cylindrical shape are provided (hereinafter, when these burner portions 17a to 17h are not particularly distinguished, they are collectively referred to as “burner portion 17”. .)
- the number of burner portions 17 provided in the partial oxidation unit 12 is not limited and may be any number as long as it is two or more. However, as the size of the partial oxidation portion 12 increases, it is preferable to increase the number to provide even groups such as 4, 6, 8,... .
- the eight burner portions 17 are provided on a reference plane P1 parallel to the horizontal plane, and are arranged at equal intervals around the central axis C2 of the partial oxidation portion 12.
- the burner portion 17 has the same direction as the virtual circle E centered on the central axis C2 with the axis C1 of the burner portion 17 smaller than the inner diameter R1 of the partial oxidation portion 12 when viewed from above D1. It arrange
- contacting around the same direction F1 means that the axis C1 contacts the virtual circle E around the direction F1 when the axis C1 of each burner portion 17 is assumed to extend from the tip of the burner portion 17.
- the axis C1 of each burner part 17 may be arrange
- the diameter ratio which is the ratio of the virtual circle diameter R2 to the internal diameter R1 of the partial oxidation portion 12 (the virtual circle diameter R2 / the internal diameter R1 of the reaction vessel), is set to be 1/10 or more and 1/3 or less. ing. The diameter ratio is more preferably 1/5 or more and 3/10 or less. Furthermore, as shown in FIG. 2, the angle ⁇ of the axis C1 of the burner portion 17 with respect to the horizontal plane is set to be 0 ° or more and 10 ° or less.
- the tip of the burner part 17 is inclined at 0 ° or more and 10 ° or less, more preferably 0 ° or more and 2 ° or less, with respect to the horizontal plane toward the lower side of the partial oxidation part 12.
- the finely pulverized coal pulverized and dried in the coal pulverization / drying facility 2 is supplied by the coal supply unit 20 to each burner unit 17 at a predetermined flow rate.
- the oxygen gas separated by the air separation equipment 9 and the water vapor supplied by the heat recovery equipment 5 as will be described later are supplied to each burner section 17 by the oxidant supply section 21 so as to have a predetermined flow rate.
- the mass flow rates of coal and oxidant (oxygen gas and water vapor) supplied from the burner unit 17 into the partial oxidation unit 12 are m1 (kg / s), m2 (kg / s),
- the flow rates of coal and oxidant at V are defined as V1 (m / s) and V2 (m / s).
- the coal supply unit 20 and the oxidant supply unit 21 are set so that the average flow velocity Va (m / s) according to the following formula (2) is 10 (m / s) or more and 50 (m / s) or less.
- Va (m1 ⁇ V1 + m2 ⁇ V2) / (m1 + m2) (2) That is, the average flow velocity Va is an average flow velocity of the fluid injected from the raw material injection port of the burner unit 17.
- oxygen gas in the oxidizing agent is 0.7 to 0.9 in terms of weight ratio of oxygen and coal (oxygen / coal)
- water vapor is 0.05 to 0 in terms of weight ratio of water vapor to coal (steam / coal).
- the flow rate V1 (m / s) of the oxidant in the burner unit 17 is a flow rate in a state where oxygen gas and water vapor are mixed. Differences in coal brands can be indicated by industrial analysis values, elemental analysis values, ash composition, etc. of coal.
- the average flow velocity Va is more preferably 10 (m / s) or more and 30 (m / s) or less.
- a cooling wall pipe 22 for cooling the partial oxidation section 12 is disposed on the outer peripheral surface of the partial oxidation section 12.
- the cooling wall pipe 22 includes water and saturated water (boiler-water). ) Is connected.
- the water or saturated water flowing in the cooling wall pipe 22 may be circulated in the cooling wall pipe 22 or after the partial oxidation unit 12 is heated as a boiler and becomes high-temperature steam. It may be recovered and used as steam.
- the pulverized and pressurized coal and oxidant are supplied from the burner unit 17 to the partial oxidation unit 12 at an average flow rate Va. Since the eight burner portions 17 are arranged as shown in FIG. 3, the coal and the oxidant supplied from the burner portion 17 are first rotated around the central axis C2 of the partial oxidation portion 12 as shown in FIG. It is sprayed so as to flow downward or on the same horizontal plane while turning.
- the inside of the partial oxidation part 12 is high temperature and high pressure (for example, temperature is 1200 degreeC or more and 1800 degrees C or less, and pressure is 2 Mpa or more).
- the coal becomes high temperature and is thermally decomposed to separate char from volatile gas containing tar, water vapor, etc., and the gasification of the coal results in the following chemical reaction formulas (1) to (3) High temperature carbon monoxide gas, carbon dioxide gas, and hydrogen gas, and slag (ash) are generated.
- FIG. 4 shows the flow velocity distribution of hydrogen gas, carbon monoxide gas, etc. at each part in the partial oxidation part 12 at this time.
- FIG. 4 shows the flow velocity v with respect to the position in the r direction from the central axis C2 on the reference plane P2 including the central axis C2 of the partial oxidation unit 12 shown in FIG.
- the reference plane P2 is a plane perpendicular to the reference plane P1 parallel to the horizontal plane.
- a fluid such as hydrogen gas or carbon monoxide gas rises while turning in the same direction (for example, direction F1) from the central axis C2 in the radial direction (r direction).
- the position of a certain height is any location along the height direction of the partial oxidation unit 12 and may be any position above the burner unit 17a.
- the horizontal axis indicates the position in the r direction with respect to the central axis C2
- the vertical axis indicates the flow velocity v.
- the position in the r direction is on the positive side (the burner portion 17a side with respect to the central axis C2 in FIG. 3), and the position in the r direction is on the negative side (the burner with respect to the central axis C2 in FIG. 3).
- FIG. 4 shows only the magnitude that does not consider the direction of the flow velocity v. Further, FIG. 4 shows the thickness of a slag, which will be described later, attached to the inner peripheral surface of the partial oxidation portion 12 without considering it.
- a burner unit 17 is installed in the partial oxidation unit 12 so that the diameter ratio of the virtual circle to the inner diameter of the partial oxidation unit (reaction vessel) 12 is 1/5 or more and 3/10 or less, and the average flow velocity A model of the flow velocity v when Va is 10 (m / s) or more and 30 (m / s) or less is indicated by a solid line. As indicated by the solid line in FIG.
- the position in the r direction where the position in the r direction which is the position on the axis C1 of the burner portion 17c is R2 / 2 and the position in the r direction which is the position on the axis C1 of the burner portion 17g are Near the position where ⁇ R2 / 2, the flow velocity v becomes maximum. Then, at the position where the position in the r direction which is the position of the inner peripheral surface of the partial oxidation portion 12 is R1 / 2 and the position where ⁇ R1 / 2, the flow velocity v approaches 0 and the gradient of the curve of the flow velocity v ( The absolute value of (velocity gradient) is a small value.
- the force (shearing force) at which the fluid tries to peel off the slag is obtained by multiplying the velocity gradient of the fluid flow velocity v by the fluid viscosity coefficient ⁇ ( ⁇ (Dv / dr)), it can be seen that the shear force in this case is relatively small.
- the position where the flow velocity v takes the maximum value does not change as shown by the dotted line in FIG.
- the maximum value of the flow velocity v increases. Accordingly, the absolute value of the slope of the curve of the flow velocity v increases, the shearing force acting on the slag increases, and the slag becomes easy to peel off.
- the diameter C ratio exceeds 1/3 by separating the axis C1 of the burner unit 17b from the central axis C2 of the partial oxidation unit 12.
- the flow velocity distribution of the fluid is a distribution as shown by a two-dot chain line in FIG. That is, also in this case, the absolute value of the slope of the curve of the flow velocity v at the position where the position in the r direction that is the position of the inner peripheral surface of the partial oxidation portion 12 is R1 / 2 and ⁇ R1 / 2 is increased. As the shearing force acting on the slag increases, the slag is easily peeled off.
- the gas, slag, etc. generated in the partial oxidation part 12 move radially outward while turning around the central axis C2 of the partial oxidation part 12 and expand at a high temperature.
- the upward force is received by the buoyancy, and the inner peripheral surface side of the partial oxidation unit 12 is raised.
- the slag generated in the partial oxidation part 12 is in a molten state, a part of the slag S is cooled and adhered on the inner peripheral surface of the partial oxidation part 12, and the other part is below the partial oxidation part 12. It falls on the slag tap 24 provided in D2, flows out into the preheating part 15, and is collect
- heat loss the amount of heat transferred to water or the like
- the heat loss will be described with reference to FIG.
- the ratio of heat loss to other conditions with the heat loss amount being 1 (reference) when the diameter ratio is 1/3 is defined as the heat loss ratio
- heat is generated when the value of the diameter ratio exceeds 1/3.
- the loss ratio (L1) increases rapidly. This is because the distance between the axis C1 of the burner portion 17 and the inner peripheral surface of the partial oxidation portion 12 is reduced. That is, the fluid ejected from the burner portion 17 is likely to face the inner peripheral surface instead of the central portion of the partial oxidation portion 12. Therefore, the slag adhering to the inner peripheral surface of the partial oxidation part 12 becomes easy to peel off.
- the reaction rate ratio means the ratio of the reaction rate with other conditions when the reaction rate when the diameter ratio is 1/3 is 1 (reference). Then, as shown in FIG. 6, when the average flow velocity Va exceeds 50 (m / s), the slag is easily peeled off as described above, and the heat loss ratio increases rapidly.
- char is accompanied by high-temperature synthesis gas mainly composed of hydrogen gas and carbon monoxide gas from above the coal gasification furnace 4, and is supplied to the heat recovery facility 5.
- the heat recovery facility 5 steam is produced by exchanging heat between the synthesis gas conveyed from the coal gasification furnace 4 and the boiler water.
- This water vapor is supplied to the above-described coal pulverization / drying facility 2 or the like for the purpose of drying the coal.
- the synthesis gas cooled by the heat recovery facility 5 is supplied from the heat recovery facility 5 to the char recovery facility 6, and the char contained in the synthesis gas is recovered by the char recovery facility 6.
- the recovered char can be used externally as fuel or the like, but the char can also be recycled to the coal gasification furnace 4 for gasification.
- the synthesis gas that has passed through the char recovery facility 6 is supplied to the shift reaction facility 7.
- steam was supplied in the shift reaction equipment 7, and the catalyst shown by following Chemical reaction formula (4) was used.
- causes a shift reaction By this shift reaction, carbon monoxide gas is consumed and hydrogen gas is generated instead.
- the synthesis gas whose components have been adjusted by the shift reaction facility 7 is supplied to the gas purification facility 8, and carbon dioxide gas contained in the synthesis gas, gas containing sulfur as a component, and the like are recovered.
- the product synthesis gas purified by the gas purification facility 8 is supplied to the chemical synthesis facility and the like, and methane, methanol, ammonia and the like are produced.
- the burner unit 17 is swung around the central axis C ⁇ b> 2 of the reaction vessel 12 by supplying coal and an oxidant into the cylindrical reaction vessel 12. A flow can be generated. For this reason, the fluid flow in the vicinity of the inner peripheral surface of the reaction vessel 12 is stabilized regardless of the position in the circumferential direction, and the molten slag generated by the gasification of coal adheres to the inner peripheral surface of the reaction vessel 12. The thickness can be made substantially uniform.
- the burner part 17 is arrange
- the burning coal that expands by gasification and is going to rise while turning in the partial oxidation unit 12 is once directed horizontally or downward D2 from the burner unit 17 before moving to the heat recovery facility 5.
- the burner part 17 is arrange
- the burner part 17 is arrange
- the inner peripheral surface of the partial oxidation portion 12 is exposed to high temperatures and being damaged. Further, by setting the diameter ratio to 1/10 or more, the coal and the oxidant supplied from the burner unit 17 are prevented from colliding with each other from the front, and turn around the central axis C2 of the partial oxidation unit 12. It is possible to reliably generate a flow and prevent the reaction rate ratio from being reduced.
- the shape of the burner portion 17 is a cylindrical shape, but may be a flat cylindrical shape, a rectangular tube shape, or the like as long as the shape extends along a predetermined axis.
- the flow of the fluid in the partial oxidation unit 12 is a swirling flow even if the burner unit 17 is not arranged at equal intervals around the central axis C2 of the partial oxidation unit 12, so the burner unit 17 may not be arranged at equal intervals around the central axis C2.
- the char burner is arranged in the same manner as the burner unit 17 on the second reference plane parallel to the reference plane P ⁇ b> 1 immediately above the burner unit 17 in the partial oxidation unit 12. May be. That is, when viewed from above D1, the char burner is arranged so that the axis of the char burner is smaller than the inner diameter R1 of the partial oxidation portion 12 and is in contact with a virtual circle centered on the central axis C2 around the same direction. Good. Furthermore, the char burner may be arranged so that the axis of the char burner is parallel to the horizontal plane or goes downward as it goes toward the tip of the char burner.
- coal is blown into the synthesis gas which has a thermal decomposition part in the upper part of the partial oxidation part 12, and has the high temperature hydrogen gas and carbon monoxide gas from the partial oxidation part 12 as a main component, Gas heat may be used for pyrolysis.
- the inner peripheral surface has a diameter of 0.65 (m) and an internal height of 1.0 (m), and the partial oxidation unit 12 has 4 at regular intervals.
- a basic burner portion 17 was provided. And it tested using the bituminous coal of 5% of ash for coal. When the average flow velocity Va of the burner portion 17 was 30 (m / s) and the diameter ratio was changed from 1/3 to 1/5, the diameter ratio was 1/3 when the diameter ratio was 1/5. It was found that the heat loss transferred from the partial oxidation unit 12 to the water in the cooling wall pipe 22 is reduced by about 20%.
- the coal gasification furnace 4 having the shape of the above-described embodiment, when the diameter ratio is 1/4 and the average flow rate Va is 10 (m / s) and the coal is gasified and operated with 1% ash, the partially oxidized portion is operated. It was found that the slag thickness adhering to the 12 inner peripheral surfaces can be kept constant. However, the above heat loss is equivalent to the case where the ash content is 3% or more when the ash content is 3% or more. However, when the ash content is 5%, the heat loss is reduced by about 30% from the case where the ash content is 1%. ing.
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
Abstract
Description
本願は、2010年4月16日に、日本に出願された特願2010-095496号に基づき優先権を主張し、その内容をここに援用する。 The present invention relates to a coal gasification furnace that produces combustible gas by gasifying coal with an oxidizing agent such as oxygen gas or water vapor.
This application claims priority based on Japanese Patent Application No. 2010-095496 filed in Japan on Apr. 16, 2010, the contents of which are incorporated herein by reference.
空気、チャー(未ガス化石炭残滓または熱分解残滓)、燃料用石炭はそれぞれのノズル内で旋回したあとで、軽油バーナーで着火されて圧力容器内に噴射される。 The combustor burner consists of a light oil burner for gasifier start-up provided in the center, and an air nozzle, char nozzle, fuel coal nozzle, and secondary air nozzle arranged concentrically with the light oil burner from the inside to the outside. It is configured.
Air, char (ungasified coal residue or pyrolysis residue), and fuel coal are swung in their respective nozzles, then ignited by a light oil burner and injected into a pressure vessel.
さらに、ガス化によって生じたガス等はガス化炉内を上昇するが、ガス化炉内におけるガス等の上昇する流れの不均一が生じたりすると、石炭中のカーボン(チャー)が十分にガス化反応する前にガス化炉から流出してしまい、反応率(石炭中の炭素のガスへの転換率)が低下してしまうことがある。 However, in the gasification furnace shown in the above-mentioned
Furthermore, gas generated by gasification rises in the gasification furnace, but if the flow of gas in the gasification furnace rises unevenly, carbon (char) in the coal is sufficiently gasified. Before it reacts, it may flow out of the gasifier and the reaction rate (conversion rate of carbon in coal to gas) may decrease.
本発明の石炭ガス化炉は、
上方に延びる円筒状に形成され上端側に排出口が設けられた反応容器と、
水平面に平行で前記排出口より下方に位置する基準平面上であって前記反応容器の内周面上に周方向に間隔を開けて複数設けられ、前記反応容器内に石炭および酸化剤を供給する筒状のバーナー部と、を備え、
前記石炭を前記反応容器内でガス化させることで少なくとも水素ガスおよび一酸化炭素ガスを製造する石炭ガス化炉において、
それぞれの前記バーナー部は、上方からみたときに、自身の軸線が前記反応容器の内径よりも小径で前記中心軸線を中心とする仮想円に同一方向回りに接するとともに、自身の軸線が水平面に平行に、または前記バーナー部の先端に向かうほど下方に向かうように配置されていることを特徴としている。
即ち、本発明では、石炭を反応容器内でガス化させることで少なくとも水素ガスおよび一酸化炭素ガスを製造する石炭ガス化炉が、
上方に延びる円筒状に形成した反応容器と、
前記反応容器の上端側設けられた排出口と、
前記反応容器内に石炭および酸化剤を供給する複数の筒状のバーナー部とを有し、
前記複数のバーナー部は、前記排出口より下方に位置する水平面に平行な基準平面上で、前記反応容器の内周面の周方向に向けて間隔を開けて設けられ、
前記反応容器の上方からみて、前記各バーナー部の軸線が、前記反応容器の中心軸線を中心としている反応容器の内径よりも径の小さい仮想円に、同一方向回りに接するように、前記各バーナー部を配置し、
前記バーナー部が、前記バーナー部の軸線が水平面に平行に、または前記バーナー部の先端に向かうほど下方に向かうように配置されていることを特徴とする。 In order to solve the above problems, the present invention proposes the following means.
The coal gasifier of the present invention is
A reaction vessel formed in a cylindrical shape extending upward and provided with a discharge port on the upper end side;
A plurality of a plurality of flat plates are provided on a reference plane that is parallel to a horizontal plane and located below the discharge port and spaced circumferentially on the inner peripheral surface of the reaction vessel, and supplies coal and an oxidant into the reaction vessel. A cylindrical burner, and
In a coal gasification furnace for producing at least hydrogen gas and carbon monoxide gas by gasifying the coal in the reaction vessel,
When viewed from above, each of the burner parts has its own axis smaller than the inner diameter of the reaction vessel and is in contact with a virtual circle centered on the center axis in the same direction, and its own axis is parallel to the horizontal plane. Alternatively, it is arranged so as to be directed downward toward the tip of the burner portion.
That is, in the present invention, a coal gasification furnace that produces at least hydrogen gas and carbon monoxide gas by gasifying coal in a reaction vessel,
A reaction vessel formed in a cylindrical shape extending upward;
An outlet provided on the upper end side of the reaction vessel;
A plurality of cylindrical burner portions for supplying coal and oxidant into the reaction vessel;
The plurality of burner portions are provided on a reference plane parallel to a horizontal plane located below the discharge port, with an interval in the circumferential direction of the inner peripheral surface of the reaction vessel,
When viewed from above the reaction vessel, each burner portion has an axis line in contact with a virtual circle having a diameter smaller than the inner diameter of the reaction vessel centered on the central axis line of the reaction vessel, in the same direction. Place the part,
The burner portion is arranged such that an axis of the burner portion is parallel to a horizontal plane or is directed downward toward the tip of the burner portion.
また、バーナー部は、自身の軸線が水平面に平行に、またはバーナー部の先端に向かうほど下方に向かうように配置されている。ガス化して膨張し、反応容器内を旋回しながら上昇しようとする石炭を、バーナー部から一度水平または下方に向かうように流すことにより、石炭が反応容器中を流れる時間を増加させ、排出口から排出される前に反応容器内で十分にガス化させることができる。 According to this invention, when coal and an oxidizing agent are supplied into a reaction vessel having a cylindrical burner portion, a flow of fluid swirling around the central axis of the reaction vessel can be generated. For this reason, the flow of the fluid in the vicinity of the inner peripheral surface of the reaction vessel is stable at any position in the circumferential direction, and molten slag generated by gasification of coal adheres to the inner peripheral surface of the reaction vessel. The thickness can be made substantially uniform.
Moreover, the burner part is arrange | positioned so that an own axis line may go to the downward direction, so that it may go in parallel with a horizontal surface, or the tip of a burner part. The coal is expanded by gasification, and the coal that is going to rise while swirling in the reaction vessel is made to flow horizontally or downward once from the burner section, thereby increasing the time for the coal to flow through the reaction vessel and from the discharge port. The gas can be sufficiently gasified in the reaction vessel before being discharged.
この発明によれば、反応容器内における、バーナー部から供給される石炭および酸化剤、そして石炭の燃焼により生じるガスを含む流体の流れをより安定させることができる。 Moreover, in the above coal gasification furnace, it is more preferable that the burner portions are arranged at regular intervals around the central axis of the reaction vessel.
According to the present invention, the flow of fluid containing coal and oxidant supplied from the burner section and gas generated by combustion of coal in the reaction vessel can be further stabilized.
この発明によれば、反応容器の内径に対する仮想円の直径の比(以下、「直径比」とも称する。)を1/3以下とすることで、反応容器の内周面における流体の速度勾配を小さくし、反応容器の内周面に付着したスラグが内周面から剥がれるのが抑えられる。したがって、反応容器の内周面が高温下にさらされて、熱損失の増加により性能が低下することや内周面が損傷するのを防止することができる。
また、直径比を1/10以上とすることで、バーナー部から供給される石炭および酸化剤等が互いに正面から衝突するのを防止して、反応容器の中心軸線回りに旋回する流れを確実に生じさせ、ガス化反応時間を長くし、反応率を向上することができる。 In the above coal gasification furnace, the ratio of the diameter of the virtual circle to the inner diameter of the reaction vessel is more preferably set to 1/10 or more and 1/3 or less.
According to this invention, by setting the ratio of the diameter of the virtual circle to the inner diameter of the reaction vessel (hereinafter also referred to as “diameter ratio”) to 1/3 or less, the velocity gradient of the fluid on the inner peripheral surface of the reaction vessel can be obtained. It is made small and it is suppressed that the slag adhering to the internal peripheral surface of reaction container peels from an internal peripheral surface. Therefore, it is possible to prevent the inner peripheral surface of the reaction vessel from being exposed to a high temperature, thereby reducing the performance due to an increase in heat loss and damaging the inner peripheral surface.
Further, by setting the diameter ratio to 1/10 or more, coal and oxidant supplied from the burner portion are prevented from colliding with each other from the front, and the flow swirling around the central axis of the reaction vessel is ensured. As a result, the gasification reaction time can be lengthened and the reaction rate can be improved.
Va=(m1×V1+m2×V2)/(m1+m2) ・・(1)
この発明によれば、平均流速Vaを50(m/s)以下とすることで、反応容器の内周面に付着したスラグが内周面から剥がれるのが抑えられて反応容器から外部に伝えられる熱損失を低下させることができる。また、平均流速Vaを10(m/s)以上とすることで、バーナー部において酸化剤により石炭を安定して搬送させることができる。 In the above coal gasification furnace, mass flow rates of the coal and the oxidant supplied from the burner portions into the reaction vessel are m1 (kg / s) and m2 (kg / s), respectively. When the flow rates of the coal and the oxidizer in the burner part are V1 (m / s) and V2 (m / s), the average flow rate Va (m / s) according to the equation (1) is 10 (m / S) and more preferably 50 (m / s) or less.
Va = (m1 × V1 + m2 × V2) / (m1 + m2) (1)
According to this invention, by setting the average flow velocity Va to 50 (m / s) or less, it is possible to suppress the slag adhering to the inner peripheral surface of the reaction vessel from being peeled off from the inner peripheral surface and to be transmitted from the reaction vessel to the outside. Heat loss can be reduced. Moreover, coal can be stably conveyed with an oxidizing agent in a burner part because average flow velocity Va shall be 10 (m / s) or more.
この発明によれば、この角度を0°以上且つ10°以下とすることで、バーナー部より吹き込んだ石炭粒子をバーナー部近傍の高温場に長く存在させることができるので、チャーのガス化反応が促進され、反応率を上昇させることができる。 In the above coal gasification furnace, the angle of the axis of each burner part with respect to the horizontal plane is more preferably set to 0 ° or more and 10 ° or less.
According to the present invention, by setting the angle to 0 ° or more and 10 ° or less, the coal particles blown from the burner part can exist in the high-temperature field near the burner part for a long time. It is promoted and the reaction rate can be increased.
この発明によれば、反応容器のチャーバーナーによって未反応で回収されたチャーを石炭ガス化炉へリサイクルさせてガス化反応をさせることで、石炭中のカーボンのガス化反応率を99%以上とすることができる。 Further, in the above coal gasification furnace, a char burner is arranged in the same manner as the burner portion on the second reference plane parallel to the reference plane and immediately above the burner portion in the reaction vessel. More preferably.
According to this invention, the char gasification reaction rate of carbon in coal is 99% or more by recycling the char recovered unreacted by the char burner of the reaction vessel to the coal gasification furnace to cause the gasification reaction. can do.
図1に示すように、石炭ガス化合成ガス製造システム1は、石炭を原料として水素ガスと一酸化炭素ガスを主成分とする合成ガスを製造するプラント設備である。この製品合成ガスを化学合成設備等の原料として供給することで、最終的にメタン、メタノールおよびアンモニア等を製造することができる。
石炭ガス化合成ガス製造システム1は、石炭粉砕・乾燥設備2と、石炭供給設備3と、本実施形態の石炭ガス化炉4と、熱回収設備5と、チャー回収設備6と、シフト反応設備7と、ガス精製設備8と、空気分離設備9とを備えている。 Hereinafter, an embodiment of a coal gasifier according to the present invention will be described with reference to FIGS. 1 to 6. A coal gasification furnace is an apparatus that is used by being incorporated in a part of a coal gasification system, and that produces at least hydrogen gas and carbon monoxide gas by burning coal inside.
As shown in FIG. 1, the coal gasification synthesis
A coal gasification synthesis
続いて、石炭は、石炭ガス化炉4内に供給するために石炭供給設備3内で搬送ガス等により所定の圧力まで昇圧され、その後で石炭ガス化炉4に気流搬送にて所定の重量が定量供給される。石炭ガス化炉の運転圧力は特に限定されないが、ガス化炉のコンパクト化による反応効率の向上、設備費及び用役費低減の観点から、2MPaG以上且つ5MPaG以下であることが望ましい。
一方で、空気分離設備9は、空気を圧縮して液化し、液体となった空気から沸点の違いにより乾燥した酸素ガスや窒素ガス等を分離する。空気分離設備9で分離された酸素ガスは、石炭ガス化炉4に所定流量供給される。 In general, the outer diameter of coal is not uniform, and depending on the type, coal may contain more water than desired. Therefore, first, in the coal pulverization /
Subsequently, in order to supply the coal into the
On the other hand, the
なお、部分酸化部12に設けられるバーナー部17の数に制限はなく、2つ以上であれば幾つでもよい。ただし、部分酸化部12の大きさが大きくなるのに応じて、4基、6基、8基、‥、というように、数を増やして偶数基設けることが好ましいが、奇数基でも全く問題ない。
8基のバーナー部17は、水平面に平行な基準平面P1上設けられるとともに、部分酸化部12の中心軸線C2回りに等間隔毎に配置されている。 As shown in FIGS. 2 and 3, the
Note that the number of
The eight
そして、部分酸化部12の内径R1に対する仮想円の直径R2の比(仮想円の直径R2/反応容器の内径R1)である直径比が1/10以上且つ1/3以下となるように設定されている。直径比はより好ましくは1/5以上且つ3/10以下である。
さらに、図2に示すように、バーナー部17の軸線C1の水平面に対する角度θが、0°以上且つ10°以下となるように設定されている。
即ち、バーナー部17の先端が、部分酸化部12の下方に向けて、水平面に対して0°以上かつ10°以下であることが好ましく、より好ましくは0°以上且つ2°以下傾いている。 As shown in FIG. 3, the
The diameter ratio, which is the ratio of the virtual circle diameter R2 to the internal diameter R1 of the partial oxidation portion 12 (the virtual circle diameter R2 / the internal diameter R1 of the reaction vessel), is set to be 1/10 or more and 1/3 or less. ing. The diameter ratio is more preferably 1/5 or more and 3/10 or less.
Furthermore, as shown in FIG. 2, the angle θ of the axis C1 of the
That is, it is preferable that the tip of the
より詳しく説明すると、バーナー部17から部分酸化部12内に供給される石炭、酸化剤(酸素ガスおよび水蒸気)の質量流量をm1(kg/s)、m2(kg/s)、バーナー部17内での石炭、酸化剤の流速をV1(m/s)、V2(m/s)とする。このとき、下記の(2)式による平均流速Va(m/s)が、10(m/s)以上且つ50(m/s)以下となるように、石炭供給部20および酸化剤供給部21により、石炭及び酸化剤の流量が調節されている。
Va=(m1×V1+m2×V2)/(m1+m2) ・・(2)
即ち、平均流速Vaとはバーナー部17の原料噴射口から射出される流体の平均流速である。
ただし、酸化剤中の酸素ガスは、酸素と石炭の重量比(酸素/石炭)で0.7~0.9、水蒸気は、水蒸気と石炭の重量比(水蒸気/石炭)で0.05~0.3の範囲で、石炭銘柄や運転計画温度にて適切に設定される。また、バーナー部17内の酸化剤の流速V1(m/s)は、酸素ガスおよび水蒸気の混合された状態での流速とする。石炭銘柄の違いは、石炭の工業分析値及び元素分析値、灰組成等で示すことが出来る。
また、平均流速Vaは、10(m/s)以上且つ30(m/s)以下であることがより好ましい。 The finely pulverized coal pulverized and dried in the coal pulverization /
More specifically, the mass flow rates of coal and oxidant (oxygen gas and water vapor) supplied from the
Va = (m1 × V1 + m2 × V2) / (m1 + m2) (2)
That is, the average flow velocity Va is an average flow velocity of the fluid injected from the raw material injection port of the
However, oxygen gas in the oxidizing agent is 0.7 to 0.9 in terms of weight ratio of oxygen and coal (oxygen / coal), and water vapor is 0.05 to 0 in terms of weight ratio of water vapor to coal (steam / coal). Within the range of .3, it is set appropriately according to the coal brand and the planned operation temperature. Further, the flow rate V1 (m / s) of the oxidant in the
The average flow velocity Va is more preferably 10 (m / s) or more and 30 (m / s) or less.
C+O2→CO2 ・・・(2)
C+H2O→CO+H2 ・・・(3) 2C + O 2 → 2CO (1)
C + O 2 → CO 2 (2)
C + H 2 O → CO + H 2 (3)
図4中に実線で示す通り、バーナー部17cの軸線C1上の位置となるr方向の位置がR2/2となる位置付近、およびバーナー部17gの軸線C1上の位置となるr方向の位置が-R2/2となる位置付近で、流速vが最大となる。そして、部分酸化部12の内周面の位置となるr方向の位置がR1/2となる位置、および-R1/2となる位置で、流速vが0に近づくとともに流速vの曲線の傾き(速度勾配)の絶対値は小さな値となる。
水素ガスや一酸化炭素ガス等がニュートン流体と仮定したときには、流体がスラグを剥がそうとする力(剪断力)は、流体の流速vの速度勾配に流体の粘性係数μを掛けたもの(μ(dv/dr))になるので、この場合の剪断力は比較的小さいことが分かる。 In FIG. 4, a
As indicated by the solid line in FIG. 4, the position in the r direction where the position in the r direction which is the position on the axis C1 of the
When hydrogen gas or carbon monoxide gas is assumed to be a Newtonian fluid, the force (shearing force) at which the fluid tries to peel off the slag is obtained by multiplying the velocity gradient of the fluid flow velocity v by the fluid viscosity coefficient μ (μ (Dv / dr)), it can be seen that the shear force in this case is relatively small.
また、実線で示された流体の流速分布を示す部分酸化部12の構成に対して、バーナー部17bの軸線C1を部分酸化部12の中心軸線C2から離間させて直径比が1/3を超えた比較例では、流体の流速分布は図4中に二点鎖線で示すような分布になる。すなわち、この場合においても、部分酸化部12の内周面の位置となるr方向の位置がR1/2および-R1/2となる位置での流速vの曲線の傾きの絶対値が増加してスラグに作用する剪断力が増加することで、スラグが剥がれやすくなる。 On the other hand, in the comparative example in which the average flow velocity Va according to the equation (2) exceeds 50 (m / s), the position where the flow velocity v takes the maximum value does not change as shown by the dotted line in FIG. The maximum value of the flow velocity v increases. Accordingly, the absolute value of the slope of the curve of the flow velocity v increases, the shearing force acting on the slag increases, and the slag becomes easy to peel off.
Further, with respect to the configuration of the
なお、部分酸化部12の内周面に付着したスラグSが厚くなるほど、スラグSによる断熱効果が増して部分酸化部12が高熱から保護されるとともに、部分酸化部12から冷却壁管路22内の水等に伝えられる熱量(以下、「熱損失」と称する。)が低減される。 As shown in FIG. 2, the gas, slag, etc. generated in the
In addition, as the slag S adhering to the inner peripheral surface of the
そして、上記の平均流速Vaは、図6に示すように、値が50(m/s)を超えると、上述のようにスラグが剥がれやすくなり熱損失比が急激に大きくなる。また、平均流速Vaが10(m/s)未満になると、石炭供給設備3からバーナー部17を介して石炭ガス化炉4内への石炭の気流搬送が不安定もしくは閉塞により不能となり、部分酸化部12への石炭供給量が変動してしまう。 Here, the heat loss will be described with reference to FIG. When the ratio of heat loss to other conditions with the heat loss amount being 1 (reference) when the diameter ratio is 1/3 is defined as the heat loss ratio, heat is generated when the value of the diameter ratio exceeds 1/3. The loss ratio (L1) increases rapidly. This is because the distance between the axis C1 of the
Then, as shown in FIG. 6, when the average flow velocity Va exceeds 50 (m / s), the slag is easily peeled off as described above, and the heat loss ratio increases rapidly. Further, when the average flow velocity Va becomes less than 10 (m / s), the air flow of coal from the
熱回収設備5では、石炭ガス化炉4から搬送された合成ガスとボイラ水とを熱交換させることにより水蒸気が製造される。この水蒸気は前述の石炭粉砕・乾燥設備2等に石炭の乾燥等の目的のために供給される。
熱回収設備5で冷却された合成ガスは、熱回収設備5からチャー回収設備6に供給され、チャー回収設備6で合成ガスに含まれるチャーが回収される。ここで、回収されたチャーは、燃料等として外部利用することもできるが、このチャーを石炭ガス化炉4にリサイクルさせてガス化することもできる。
チャー回収設備6を通過した合成ガスは、シフト反応設備7に供給される。そして、合成ガス中の一酸化炭素ガスに対する水素ガスの比率を一定の値まで高めるために、シフト反応設備7中に水蒸気を供給し、下記の化学反応式(4)で示される触媒を用いたシフト反応を生じさせる。このシフト反応により、一酸化炭素ガスが消費されて代わりに水素ガスが発生する。 Then, as shown in FIG. 1, char is accompanied by high-temperature synthesis gas mainly composed of hydrogen gas and carbon monoxide gas from above the
In the
The synthesis gas cooled by the
The synthesis gas that has passed through the
ガス精製設備8で精製された製品合成ガスは、化学合成設備等に供給され、メタンやメタノール及びアンモニア等が製造される。 The synthesis gas whose components have been adjusted by the shift reaction facility 7 is supplied to the
The product synthesis gas purified by the
また、バーナー部17は、自身の軸線C1が水平面に平行に、またはバーナー部の先端に向かうほど下方D2に向かうように配置されている。この構成によれば、ガス化して膨張し、部分酸化部12内を旋回しながら上昇しようとする燃焼する石炭を、熱回収設備5に移動する前にバーナー部17から一度水平または下方D2に向かうように流すことができる。従って、バーナー部17より吹き込んだ石炭粒子をバーナー部17近傍の高温場に長く存在させることができ、さらには、石炭中のカーボン(チャー)が部分酸化部12中を流れる時間を増加させることができるので、部分酸化部12内で十分にガス化させることができる。 As described above, in the
Moreover, the
また、バーナー部17は、反応容器の内径に対する仮想円の直径比が1/10以上1/3以下となるように配置されている。直径比を1/3以下とすることで、部分酸化部12の内周面における流体の速度勾配を小さくし、部分酸化部12の内周面に付着した溶融したスラグ等が内周面から剥がれるのが抑えられる。したがって、部分酸化部12の内周面が高温下にさらされて損傷するのを防止することができる。さらに、直径比を1/10以上とすることで、バーナー部17から供給される石炭および酸化剤等が互いに正面から衝突するのを防止して、部分酸化部12の中心軸線C2回りに旋回する流れを確実に生じさせ、反応率比が小さくなることを防止することができる。 And since the
Moreover, the
また、バーナー部17の軸線C1の水平面に対する角度θを0°以上且つ10°以下とすることで、バーナー部17より吹き込んだ石炭粒子をバーナー部17近傍の高温場に長く存在させることができるので、石炭中のカーボンのガス化反応が促進され、反応率を上昇させることができる。 And by making average flow velocity Va into 50 (m / s) or less, it is suppressed that the slag adhering to the internal peripheral surface of the
Moreover, since the angle θ of the axis C1 of the
たとえば、上記実施形態では、バーナー部17の形状を円筒状としたが、所定の軸線に沿って延びる形状であれば、扁平した円筒状や角筒状等でもよい。
また、上記実施形態では、バーナー部17は部分酸化部12の中心軸線C2回りに等間隔毎に配置されていなくても部分酸化部12内の流体の流れは旋回する流れになるので、バーナー部17は中心軸線C2回りに等間隔毎に配置されていなくてもよい。 As mentioned above, although embodiment of this invention was explained in full detail with reference to drawings, the concrete structure is not restricted to this embodiment, The change of the structure of the range which does not deviate from the summary of this invention, etc. are included.
For example, in the above embodiment, the shape of the
Further, in the above embodiment, the flow of the fluid in the
尚、上記リサイクルに関しては、チャーバーナーを使用せずチャーを石炭に均一に混合したものをバーナー部17に供給してもよい。
さらに、上記実施形態では、部分酸化部12の上部に、熱分解部を備えて部分酸化部12からの高温の水素ガスおよび一酸化炭素ガスを主成分とする合成ガスに石炭を吹き込み、上記合成ガスの熱を熱分解に利用してもよい。 In the above coal gasification furnace, the char burner is arranged in the same manner as the
In addition, regarding the said recycling, you may supply to the
Furthermore, in the said embodiment, coal is blown into the synthesis gas which has a thermal decomposition part in the upper part of the
バーナー部17の平均流速Vaを30(m/s)として、直径比を1/3から1/5に変えて運転したところ、直径比が1/5とした方が、直径比が1/3とした場合に対して部分酸化部12から冷却壁管路22内の水等に伝えられる上記の熱損失が約20%低減することが分かった。
また、部分酸化部12の直径比を1/3に固定して、バーナー部17の平均流速Vaを50(m/s)から30(m/s)に変えて運転したところ、平均流速Vaが30(m/s)のときの方が、平均流速Vaが50(m/s)のときに対して熱損失が約10%低減することが分かった。
そして、直径比を1/3から1/5に変えるとともに、平均流速Vaを50(m/s)から30(m/s)に変えて運転したときには、熱損失が約20%低下した。 In the
When the average flow velocity Va of the
Moreover, when the diameter ratio of the
When the diameter ratio was changed from 1/3 to 1/5 and the average flow velocity Va was changed from 50 (m / s) to 30 (m / s), the heat loss was reduced by about 20%.
ただし、上記の熱損失は、灰分が3%以上であれば灰分が5%の場合と同等であるが、灰分が5%の場合は灰分が1%の場合より約30%低下することが分かっている。 Further, in the
However, the above heat loss is equivalent to the case where the ash content is 3% or more when the ash content is 3% or more. However, when the ash content is 5%, the heat loss is reduced by about 30% from the case where the ash content is 1%. ing.
12 部分酸化部(反応容器)
17a~17h バーナー部
C1 軸線
C2 中心軸線
E 仮想円
P1 基準平面
θ 角度 4
17a to 17h Burner section C1 axis C2 center axis E virtual circle P1 reference plane θ angle
Claims (5)
- 石炭を反応容器内でガス化させることで少なくとも水素ガスおよび一酸化炭素ガスを製造する石炭ガス化炉が、
上方に延びる円筒状に形成した反応容器と、
前記反応容器の上端側設けられた排出口と、
前記反応容器内に石炭および酸化剤を供給する複数の筒状のバーナー部とを有し、
前記複数のバーナー部は、前記排出口より下方に位置する水平面に平行な基準平面上で、前記反応容器の内周面の周方向に向けて間隔を開けて設けられ、
前記反応容器の上方からみて、前記各バーナー部の軸線が、前記反応容器の中心軸線を中心としている反応容器の内径よりも径の小さい仮想円に、同一方向回りに接するように、前記各バーナー部を配置し、
前記バーナー部が、前記バーナー部の軸線が水平面に平行に、または前記バーナー部の先端に向かうほど下方に向かうように配置されていることを特徴とする。 A coal gasification furnace that produces at least hydrogen gas and carbon monoxide gas by gasifying coal in a reaction vessel,
A reaction vessel formed in a cylindrical shape extending upward;
An outlet provided on the upper end side of the reaction vessel;
A plurality of cylindrical burner portions for supplying coal and oxidant into the reaction vessel;
The plurality of burner portions are provided on a reference plane parallel to a horizontal plane located below the discharge port, with an interval in the circumferential direction of the inner peripheral surface of the reaction vessel,
When viewed from above the reaction vessel, each burner portion has an axis line in contact with a virtual circle having a diameter smaller than the inner diameter of the reaction vessel centered on the central axis line of the reaction vessel, in the same direction. Place the part,
The burner portion is arranged such that an axis of the burner portion is parallel to a horizontal plane or is directed downward toward the tip of the burner portion. - 前記バーナー部は、前記反応容器の中心軸線回りに等間隔毎に配置されている請求項1に記載の石炭ガス化炉。 The coal gasifier according to claim 1, wherein the burner portions are arranged at equal intervals around the central axis of the reaction vessel.
- 前記反応容器の内径に対する前記仮想円の直径の比が、1/10以上1/3以下に設定されている請求項1または請求項2に記載の石炭ガス化炉。 The coal gasification furnace according to claim 1 or 2, wherein a ratio of a diameter of the virtual circle to an inner diameter of the reaction vessel is set to 1/10 or more and 1/3 or less.
- それぞれの前記バーナー部から前記反応容器内に供給される前記石炭、前記酸化剤の質量流量をm1(kg/s)、m2(kg/s)、それぞれの前記バーナー部内での前記石炭、前記酸化剤の流速をV1(m/s)、V2(m/s)としたときに、(1)式による平均流速Va(m/s)が、10(m/s)以上且つ50(m/s)以下に設定されている請求項1から請求項3のいずれか1項に記載の石炭ガス化炉。
Va=(m1×V1+m2×V2)/(m1+m2) ・・(1) The mass flow rate of the coal and the oxidizer supplied from the burner portions to the reaction vessel is m1 (kg / s), m2 (kg / s), the coal in the burner portions, and the oxidation, respectively. When the flow rate of the agent is V1 (m / s) and V2 (m / s), the average flow rate Va (m / s) according to the formula (1) is 10 (m / s) or more and 50 (m / s) The coal gasifier according to any one of claims 1 to 3, which is set as follows.
Va = (m1 × V1 + m2 × V2) / (m1 + m2) (1) - ぞれぞれの前記バーナー部の軸線の水平面に対する角度が、0°以上且つ10°以下に設定されている請求項1から請求項4のいずれか1項に記載の石炭ガス化炉。 The coal gasifier according to any one of claims 1 to 4, wherein an angle of an axis of each burner portion with respect to a horizontal plane is set to 0 ° or more and 10 ° or less.
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN2011800191978A CN102892870A (en) | 2010-04-16 | 2011-04-11 | Coal gasification furnace |
AU2011241999A AU2011241999B2 (en) | 2010-04-16 | 2011-04-11 | Coal gasifier |
JP2012510648A JP5552157B2 (en) | 2010-04-16 | 2011-04-11 | Coal gasifier |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2010095496 | 2010-04-16 | ||
JP2010-095496 | 2010-04-16 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2011129302A1 true WO2011129302A1 (en) | 2011-10-20 |
Family
ID=44798675
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2011/059020 WO2011129302A1 (en) | 2010-04-16 | 2011-04-11 | Coal gasification furnace |
Country Status (4)
Country | Link |
---|---|
JP (1) | JP5552157B2 (en) |
CN (2) | CN104479748B (en) |
AU (1) | AU2011241999B2 (en) |
WO (1) | WO2011129302A1 (en) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN108998097B (en) * | 2018-08-28 | 2020-11-24 | 南京六创科技发展有限公司 | Coal gasification method |
CN113319113A (en) * | 2021-05-17 | 2021-08-31 | 太原理工大学 | Thermal desorption device and process for organic contaminated soil |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS59176391A (en) * | 1983-03-28 | 1984-10-05 | Hitachi Ltd | Coal gasifying oven |
JPH0873869A (en) * | 1994-09-06 | 1996-03-19 | Mitsubishi Heavy Ind Ltd | Coal gasification furnace having two-stage jet bed |
JPH08269466A (en) * | 1995-03-29 | 1996-10-15 | Mitsubishi Heavy Ind Ltd | Entrained bed coal gasifier |
JP2002155289A (en) * | 2000-11-21 | 2002-05-28 | Nippon Steel Corp | Gas-flowing bed type method for gasifying coal |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH0295687A (en) * | 1988-09-30 | 1990-04-06 | Toshiba Corp | Display device for cage position of elevator |
JP3504772B2 (en) * | 1995-04-25 | 2004-03-08 | 三菱重工業株式会社 | Spouted bed coal gasifier |
WO1997044412A1 (en) * | 1996-05-20 | 1997-11-27 | Hitachi, Ltd. | Coal gasification apparatus, coal gasification method and integrated coal gasification combined cycle power generating system |
JPH11269471A (en) * | 1998-03-23 | 1999-10-05 | Nippon Steel Corp | Coal rapid thermal decomposition oven and method for preventing char deposition |
JP4085239B2 (en) * | 2002-02-12 | 2008-05-14 | 株式会社日立製作所 | Gasification method and gasification apparatus |
EP1896368B1 (en) * | 2005-06-28 | 2013-05-01 | Afognak Native Corporation | Method and apparatus for automated, modular, biomass power generation |
CN101392191B (en) * | 2008-10-15 | 2011-11-23 | 合肥工业大学 | Two stage type dry coal powder entrained flow gasifier |
CN101508915B (en) * | 2009-03-17 | 2012-09-05 | 惠生工程(中国)有限公司 | Gasifying device for liquid fuel or solid fuel aqueous slurry |
-
2011
- 2011-04-11 CN CN201410557701.5A patent/CN104479748B/en active Active
- 2011-04-11 WO PCT/JP2011/059020 patent/WO2011129302A1/en active Application Filing
- 2011-04-11 JP JP2012510648A patent/JP5552157B2/en active Active
- 2011-04-11 AU AU2011241999A patent/AU2011241999B2/en active Active
- 2011-04-11 CN CN2011800191978A patent/CN102892870A/en active Pending
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS59176391A (en) * | 1983-03-28 | 1984-10-05 | Hitachi Ltd | Coal gasifying oven |
JPH0873869A (en) * | 1994-09-06 | 1996-03-19 | Mitsubishi Heavy Ind Ltd | Coal gasification furnace having two-stage jet bed |
JPH08269466A (en) * | 1995-03-29 | 1996-10-15 | Mitsubishi Heavy Ind Ltd | Entrained bed coal gasifier |
JP2002155289A (en) * | 2000-11-21 | 2002-05-28 | Nippon Steel Corp | Gas-flowing bed type method for gasifying coal |
Also Published As
Publication number | Publication date |
---|---|
AU2011241999B2 (en) | 2013-12-19 |
JP5552157B2 (en) | 2014-07-16 |
CN104479748A (en) | 2015-04-01 |
AU2011241999A1 (en) | 2012-12-06 |
CN104479748B (en) | 2018-01-05 |
JPWO2011129302A1 (en) | 2013-07-18 |
CN102892870A (en) | 2013-01-23 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN100366710C (en) | Multi-nozzle coal water mixture or fine coal gasifying furnace and its industrial application | |
US20150090938A1 (en) | Method and Device for the Entrained Flow Gasification of Solid Fuels under Pressure | |
KR102203125B1 (en) | Second stage gasifier in staged gasification | |
CN101985568B (en) | Two-stage oxygen supply dry slag removal pressurized gas flow bed gasification furnace | |
JP5130459B2 (en) | Operation method of coal pyrolysis gasifier | |
JP5450800B2 (en) | Coal pyrolysis gasification method and coal pyrolysis gasification device | |
JPWO2011129192A1 (en) | Coal gasification system and coal gasification method | |
JP5552157B2 (en) | Coal gasifier | |
CN107429176B (en) | Method for operating coal gasification system | |
JP5827511B2 (en) | Coal gas production method and methane production method | |
JP3976888B2 (en) | Coal air bed gasification method and apparatus | |
EP4163352A1 (en) | Method for gasification of carbonaceous feedstock and device for implementing same | |
JP2004277647A (en) | Process for gasification of waste product and installation therefor | |
US8877097B2 (en) | Method for the generation of synthesis gas | |
JP5211369B1 (en) | Coal pyrolysis method | |
JP5639955B2 (en) | Coal gasification system | |
CN103409170A (en) | Slag blockage preventing gasification reactor with graded carbonaceous fuel feeding | |
JP5851116B2 (en) | Coal gasification system | |
JP4863889B2 (en) | Coal hydrocracking process | |
JP2009019125A (en) | Gasification method and apparatus | |
CN113897222A (en) | Gasification furnace for carbon-containing waste and gasification method for carbon-containing waste | |
JP2010254727A (en) | Airflow layer gasification furnace and method for operating the same |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201180019197.8 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 11768823 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2012510648 Country of ref document: JP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2011241999 Country of ref document: AU Date of ref document: 20110411 Kind code of ref document: A |
|
122 | Ep: pct application non-entry in european phase |
Ref document number: 11768823 Country of ref document: EP Kind code of ref document: A1 |