WO2011129192A1 - Système de gazéification de charbon et méthode de gazéification de charbon - Google Patents

Système de gazéification de charbon et méthode de gazéification de charbon Download PDF

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Publication number
WO2011129192A1
WO2011129192A1 PCT/JP2011/057482 JP2011057482W WO2011129192A1 WO 2011129192 A1 WO2011129192 A1 WO 2011129192A1 JP 2011057482 W JP2011057482 W JP 2011057482W WO 2011129192 A1 WO2011129192 A1 WO 2011129192A1
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Prior art keywords
coal
moisture
reaction vessel
water
coal gasification
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PCT/JP2011/057482
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English (en)
Japanese (ja)
Inventor
小水流　広行
小菅　克志
眞須美 糸永
矢部　英昭
卓 武田
良之 幸
泰樹 並木
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新日鉄エンジニアリング株式会社
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Priority to CN201180018831.6A priority Critical patent/CN102892869B/zh
Priority to JP2012510610A priority patent/JP5450799B2/ja
Priority to AU2011241630A priority patent/AU2011241630B2/en
Publication of WO2011129192A1 publication Critical patent/WO2011129192A1/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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow 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
    • C10J3/46—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
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • 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
    • 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
    • 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 system and a coal gasification method for producing a product such as methane using coal as a raw material.
  • a product such as methane using coal as a raw material.
  • coal having coal gasification reactors of various configurations such as fixed bed type, fluidized bed type, and fluidized bed type (jet bed) type to gasify coal and efficiently produce combustible gas etc.
  • Gasification systems are being considered.
  • a coal gasification system disclosed in Patent Document 1 is known.
  • This coal gasification system comprises a pyrolysis gasification reactor (upper reaction vessel) for pyrolyzing coal, a heat exchanger for recovering sensible heat from gas etc. generated from the pyrolysis gasification reactor, the gas, etc.
  • a desulfurizer that removes sulfur from the gas from which the char has been separated to purify the gas.
  • the pyrolysis gasification reactor is in communication with the high temperature gasification furnace (lower reaction vessel) on the lower side.
  • the high temperature gasifier is supplied with coal, an oxygen-containing gas such as oxygen or oxygen-enriched air, and water vapor.
  • the high temperature gasification furnace generates a high temperature gas mainly composed of hydrogen gas and carbon monoxide gas.
  • the pyrolysis gasification reactor is provided with a coal blowing nozzle for blowing coal into the pyrolysis gasification reactor, and a steam nozzle for adding water vapor in the pyrolysis gasification reactor. From the coal supplied from the coal blowing nozzle into the pyrolysis gasification reactor, char and volatile gas are generated by the pyrolysis reaction.
  • the char generated here is decomposed into various gases by the following chemical reaction formula.
  • Patent Document 1 describes that, among the above chemical reaction formulas, the reaction rate of the chemical reaction formula (1) is about several times faster than the reaction rate of the chemical reaction formula (2).
  • Supplying steam to make the inside of the pyrolysis gasification reactor a steam-enriched atmosphere is said to be extremely effective in decomposing char.
  • the pyrolysis of coal generates a tar mainly composed of carbon and adheres to the inside of the pyrolysis gasification reactor. If the deposition amount of tar increases, finally, a part of the pyrolysis gasification reactor may be clogged with tar, and the pyrolysis gasification reactor may not be able to operate normally.
  • this tar is also gasified by the chemical reaction of the above-mentioned chemical reaction formulas (1) and (2).
  • the deposition of tar includes the deposition of carbonaceous material derived from tar.
  • the present invention has been made in view of such problems, and it is possible to control the amount of water vapor inside the upper reaction container without requiring an apparatus for supplying water vapor to the upper reaction container.
  • the purpose is to provide a system and a coal gasification method.
  • a coal gasification system comprises drying a coal to dry a moisture-adjusting coal having a predetermined moisture content; and burning the moisture-adjusting coal And a coal gasification reactor for producing hydrogen gas and carbon monoxide gas.
  • the coal gasification reactor is provided with a lower reaction vessel; an upper reaction vessel provided above the lower reaction vessel and in communication with the lower reaction vessel; the moisture control coal and the oxygen-containing gas in the lower reaction vessel.
  • the coal is dried by the drying device to an extent having a predetermined water content to obtain the water content adjusting coal.
  • a high temperature gas mainly composed of carbon monoxide gas is generated inside the lower reaction vessel.
  • the high temperature gas generated inside the lower reaction vessel flows into the upper reaction vessel.
  • the water content adjusting coal is supplied to the upper reaction container through the nozzle unit separately from the amount supplied to the lower reaction container, and is heated by the high temperature gas flowing into the upper reaction container.
  • the moisture control coal is heated from the high temperature gas, the pyrolysis generates carbon-based tar and char.
  • the tar and char chemically react with a predetermined amount of water left in the moisture control coal to gasify (see Formula (1)).
  • coal such as subbituminous coal and lignite contains water of about 30 to 60% (weight%). Therefore, in the process of drying these, it is adjusted so that a predetermined amount of water remains, and the remaining water is used to generate water vapor to promote the gasification of tar. As a result, it is possible to prevent tar from adhering to the inside of the gasification reaction furnace without supplying steam to the upper and lower reaction vessels as in the prior art.
  • the above-mentioned coal gasification system is a pressure measurement part which measures the difference between the pressure in the furnace below the nozzle part and the pressure in the furnace above the upper reaction vessel; and the pressure difference measured by the pressure measurement part And a controller configured to control the drying device based on the above to adjust the amount of water contained in the coal.
  • the pressure measuring unit measures the difference between the pressure in the furnace below the nozzle and the pressure in the furnace above the upper reaction vessel. Then, when a pressure difference at which tar adhesion is recognized is detected, the drying device is controlled to increase the amount of water contained in the coal.
  • the water amount adjustment coal with increased water amount is heated from the high temperature gas, tar and char mainly composed of carbon are generated by thermal decomposition, and the water is vaporized to be water vapor. Tar and char chemically react with part of the generated water vapor and are gasified. Furthermore, the tar deposited on the inner surface of the reaction vessel chemically reacts with the remaining water vapor and is gasified. Thereby, it can suppress that tar adheres to the upper reaction container inner surface.
  • a coal gasification system is a drying apparatus for drying subbituminous coal or lignite containing 20% or more of moisture by mass ratio so as to contain a predetermined amount of moisture to obtain moisture-adjusted coal.
  • a coal gasification reactor for producing at least hydrogen gas and carbon monoxide gas by burning the moisture-regulated coal.
  • the coal gasification reactor has a lower reaction vessel in which a storage space is formed, and an upper reaction vessel provided above the lower reaction vessel.
  • the lower reaction vessel has a burner unit that supplies the moisture-adjusting coal and the oxygen-containing gas at a predetermined ratio without supplying water vapor to the lower reaction vessel and burns the moisture-adjusting coal.
  • the upper reaction vessel supplies only the water content adjusting coal without supplying water vapor to the upper reaction vessel, and a through hole extending in the vertical direction in communication with the storage space of the lower reaction vessel via the reduced diameter portion It has a nozzle part that The predetermined amount is set such that the water does not adhere to the through holes by chemical reaction with the tar generated from the water amount adjusting coal.
  • Subbituminous coal and lignite contain water of about 30 to 60% (weight%).
  • the subbituminous coal or the lignite is dried by the drying apparatus to be the moisture control coal, and the moisture control coal is controlled so as to contain water higher than the residual moisture in the conventional coal gasification system.
  • the chemical reaction between a predetermined amount of water of the moisture control coal and the tar generated from the moisture control coal causes a moisture control such that the tar does not adhere to the through holes. Adjust the amount of water in the coal.
  • the moisture control coal and the oxygen-containing gas are supplied at a predetermined ratio without supplying water vapor from the burner unit to the storage space in the lower reaction container to burn the moisture control coal, and Only moisture regulation coal is supplied to the through hole without supplying water vapor from the nozzle portion.
  • Both carbon and water supplied into the upper reaction vessel are contained in the moisture control coal.
  • tar and char mainly composed of carbon are formed.
  • Moisture Content The moisture in the coal is heated in the upper reaction vessel to become water vapor.
  • the tar, char and water vapor immediately after being produced from the moisture control coal are mixed.
  • these tar, char and water vapor are supplied from separate nozzles, the tar and char and the water vapor may be incapable of reacting due to their separated positions.
  • the tar, char and water vapor are mixed, it is possible to prevent them from becoming unreactive.
  • the amount of water contained in the amount-of-water control coal supplied into the upper reaction vessel is controlled by the drying device, and the tar and steam generated by the thermal decomposition of the amount-of-water control coal react with each other to cause through holes.
  • the tar and steam generated by the thermal decomposition of the amount-of-water control coal react with each other to cause through holes.
  • prescribed water content may be set to mass ratio 15%-40% by content in the said water content adjustment coal.
  • the reaction between tar and water vapor in the upper reaction vessel is further promoted, and tar does not adhere to the through holes. can do.
  • the coal gasification reaction furnace is an internal pressure of a portion below the nozzle portion in the through hole of the upper reaction container or an internal pressure of a storage space of the lower reaction container, and the through hole
  • the pressure measurement unit may be configured to measure a pressure difference between the pressure at the upper end portion of
  • the coal gasification system may include a control unit that controls the drying device to adjust the water content of the coal based on the pressure difference measured by the pressure measurement unit. In this case, even if tar generated by thermal decomposition of coal adheres to the upper reaction vessel, the tar is concentrated at a position vertically above the nozzle portion in the through hole of the upper reaction vessel. Adhere to.
  • the control unit can promote the chemical reaction between the tar and the steam by increasing the amount of water in the moisture control coal, and can gasify the tar deposited in the through holes of the upper reaction vessel .
  • the coal gasification method implements the following steps using the coal gasification system described in any of the above.
  • the water content adjusting coal and the oxygen-containing gas are supplied to the lower reaction container without supplying steam from the burner part, and the water content adjusting coal is burned, and the upper reaction container is fed with the water from the nozzle part.
  • a chemical reaction process in which only the water amount adjusting coal is supplied to cause a chemical reaction of the water amount adjusting coal.
  • the coal is dried to obtain a moisture control coal containing a predetermined moisture content; and the water control coal in the lower reaction vessel of the coal gasification reactor.
  • the amount of water vapor in the upper reaction container can be adjusted without requiring an apparatus for supplying water vapor to the upper reaction container.
  • FIG. 1 It is a block diagram of a coal gasification system concerning a 1st embodiment of the present invention. It is the figure which fractured a part of principal part of the same coal gasification system. It is sectional drawing of the drying apparatus of the same coal gasification system. It is a figure which shows the change of the content of the water
  • the coal gasification system 1 synthesizes a synthesis gas containing hydrogen gas and carbon monoxide gas as main components using coal as a raw material, and from this synthesis gas, finally, methane, methanol, ammonia and the like are produced. It is a plant facility that manufactures products.
  • coal used by coal gasification system 1 of this embodiment subbituminous coal or lignite containing 20% or more of moisture by weight can be used.
  • the coal gasification system 1 includes a coal drying and pulverizing facility (drying apparatus) 2, a coal supply facility 3, a coal gasification reactor 4, a heat recovery facility 5, a char recovery facility 6, and a shift reaction facility 7. , Gas purification equipment 8, chemical synthesis equipment 9, and air separation equipment 10.
  • the coal drying and crushing facility 2 has a drying unit 13 for heating coal and a crushing unit 14 for crushing coal to a predetermined particle diameter (outer diameter).
  • coal has an uneven particle size, and subbituminous coal and brown coal contain a large amount of water of, for example, about 30 to 60% by mass ratio. Therefore, the sub-bituminous coal or lignite has a predetermined moisture content by grinding the sub-bituminous coal or lignite heated in the drying unit 13 into particles having a particle diameter of, for example, about 10 ⁇ m to 100 ⁇ m in the crushing unit 14. Adjust as. In this manner, a moisture-regulated coal having a predetermined moisture content is produced from coal having a moisture content of about 30 to 60% by mass ratio.
  • the drying unit 13 and the crushing unit 14 both function as a drying apparatus for drying coal.
  • the moisture content of granular moisture control coal produced by the coal drying and pulverizing facility 2 is set to be 15% or more and 40% or less by mass ratio, which is lower than the moisture content of coal before drying.
  • the measurement of the moisture content of coal before drying and the measurement of the moisture content of dried and pulverized water can be performed using, for example, an infrared moisture meter. For example, by adjusting the heating temperature or heating time in the drying unit 13 or the particle size of coal after crushing in the crushing unit 14, it is possible to adjust the water content of the water amount adjusting coal.
  • the drying unit 13 is configured by a double-pipe structure of an inner cylinder 15 and an outer cylinder 16 coaxially disposed.
  • the inner cylinder 15 and the outer cylinder 16 are disposed such that the tip end side is inclined downward at a constant angle with respect to the horizontal plane.
  • a hopper 17 for introducing coal B into the inner cylinder 15 is connected to the base end side (the obliquely upper side in the vertical direction) of the inner cylinder 15.
  • a delivery mechanism 18 for delivering the coal B to the tip side (obliquely lower side in the vertical direction) is disposed.
  • a flow rate adjusting valve 19 is connected between the outer cylinder 16 and the inner cylinder 15 to supply water vapor at a constant temperature by adjusting the flow rate.
  • the steam supplied between the inner cylinder 15 and the outer cylinder 16 flows so as to face the direction in which the coal B is sent, and is discharged from the discharge pipe 20 connected to the outer cylinder 16.
  • a temperature sensor for measuring the outlet temperature of the pulverizing unit 14 is provided.
  • the drying unit 13 configured as described above operates the flow rate adjusting valve 19 while measuring with the temperature sensor of the crushing unit 14 to adjust the amount of water vapor flowing between the inner cylinder 15 and the outer cylinder 16. And, while conveying the coal B to the tip side inside the inner cylinder 15, the coal B is heated by the steam. Thereby, the amount of water contained in coal B is adjusted.
  • the method of drying coal in a drying part will not be specifically limited if the amount of moisture in coal can be adjusted.
  • a method of heating coal with steam may be used, or a method of heating using a heater or the like may be used.
  • FIG. 4 shows an example of the result of drying the coal B by the coal drying and crushing facility 2.
  • coal B is primarily dried and the water content in coal B is supplied to the drying unit 13 in a state of being dried to 25%.
  • the horizontal axis in FIG. 4 indicates the outlet temperature of the grinding unit 14 measured by the temperature sensor, and the vertical axis indicates the water content in the moisture-adjusting coal after leaving the grinding unit 14.
  • the moisture content of the moisture adjustment coal is 5%
  • the outlet temperature of the crushing unit 14 is 50 ° C.
  • the moisture content in the moisture adjustment coal is 18 %Met.
  • the outlet temperature of the crushing unit 14 becomes higher. Then, when the outlet temperature of the crushing part 14 becomes high, it is understood that the coal B is heated to a higher temperature in the inner cylinder 15, and the water content in the water amount adjusting coal discharged from the outlet of the crushing part 14 decreases. .
  • the water amount adjusting coal pulverized in the pulverizing unit 14 is mixed with the carrier gas in the coal supply facility 3 in order to be able to be supplied into the coal gasification reactor 4.
  • the carrier gas containing the moisture content adjusting coal is pressurized to a predetermined pressure and supplied to the coal gasification reaction furnace 4.
  • the moisture content adjustment coal which evaporated the fixed amount of water
  • the air separation equipment 10 shown in FIG. 1 compresses and liquefies air, and separates oxygen gas, nitrogen gas, and the like which are dried from the air that has become a liquid due to the difference in boiling point.
  • the oxygen gas separated by the air separation facility 10 is supplied to the coal gasification reactor 4.
  • the coal gasification reaction furnace 4 is an apparatus for producing at least hydrogen gas and carbon monoxide gas by burning moisture control coal inside.
  • the coal gasification reaction furnace 4 includes a partial oxidation unit (lower reaction vessel) 26 and a thermal decomposition unit (upper reaction vessel) 28 provided on the upper side D 1 in the vertical direction of the partial oxidation unit 26.
  • the partial oxidation portion 26 has a storage space 26 a formed therein.
  • the thermal decomposition section 28 has a through hole (tubular section) 27 extending in the up-and-down direction D in communication with the accommodation space 26 a of the partial oxidation section 26 via the reduced diameter section 28 a.
  • the coal gasification reaction furnace 4 is formed of a heat-resistant brick or the like.
  • a slag cooling water tank 29 is provided below the partial oxidation unit 26 at D2.
  • the partial oxidation portion 26 and the slag cooling water tank 29 communicate with each other in the vertical direction (vertical direction) D.
  • a small diameter portion whose diameter is reduced is formed at a connection portion between the partial oxidation portion 26 and the slag cooling water tank 29.
  • the partial oxidation portion 26 is formed in a substantially cylindrical shape extending in the vertical direction D.
  • a plurality of gasification burners (burner units) 30 formed in a cylindrical shape extending along the axis C1 are provided on the inner peripheral surface of the partial oxidation unit 26.
  • the gasification burner 30 is connected to the coal supply facility 3 and the air separation facility 10, and the partial oxidation unit 26 is a moisture control coal and an oxygen-containing gas, and (hereinafter referred to as "moisture control coal etc.” Can be supplied at a predetermined rate.
  • the gasification burner 30 is disposed such that its tip end side is directed obliquely downward with respect to the horizontal plane, and its axis C 1 is at a position of twist with respect to the central axis C 2 of the partial oxidation portion 26. Thereby, the gasification burner 30 is arranged such that the flow of the gas to be jetted becomes a swirling flow that swirls about the central axis C2 of the partial oxidation unit 26. Further, a cooling means (not shown) is provided on the outer peripheral surface of the partial oxidation portion 26, and the partial oxidation portion 26 heated by the combustion of the moisture content adjusting coal can be cooled.
  • the thermal decomposition section 28 is formed in a tubular or cylindrical shape extending in the up-down direction D.
  • the inner diameter of the through hole 27 is smaller than the inner diameter of the accommodation space 26 a of the partial oxidation portion 26.
  • a plurality of nozzle portions 31 for supplying only the moisture content adjusting coal to the thermal decomposition portion 28 is provided in the middle portion of the thermal decomposition portion 28 in the vertical direction D.
  • the nozzle portion 31 is connected to the coal supply facility 3.
  • the thermal decomposition unit 28 is not provided with a steam nozzle for supplying water vapor to the thermal decomposition unit as in the conventional thermal decomposition unit. Further, the number of the gasification burner 30 and the number of the nozzle portion 31 is not limited, and may be any number.
  • the end portion 27 a of the upper portion D 1 of the through hole 27 of the thermal decomposition section 28 is connected to the heat recovery facility 5.
  • the coal gasification system 1 is provided with a pressure measurement device (pressure measurement unit) 33 that measures the pressure difference in the through holes 27 of the thermal decomposition unit 28.
  • the pressure measuring device 33 has a first pipe 34, a second pipe 35, and a main body 36.
  • the first pipe 34 is connected to the accommodation space 26 a of the partial oxidation portion 26, and the second pipe 35 is connected to the end 27 a of the through hole 27.
  • the main body 36 measures a pressure difference between the internal pressure of the first pipe 34 and the internal pressure of the pipe of the second pipe 35.
  • a predetermined amount of water W is accommodated in the slag cooling water tank 29, and as described later, the slag flowing from the partial oxidation unit 26 is cooled.
  • the moisture control coal and the like are supplied from the gasification burner 30 into the partial oxidation unit 26 at a predetermined flow rate.
  • Each gasification burner 30 is arrange
  • the inside of the partial oxidation portion 26 is high temperature and high pressure (for example, the temperature is 1300 ° C. or more and 1700 ° C.
  • the gas, slag and the like generated in the partial oxidation portion 26 expand at high temperature and expand by receiving a force in the upward direction D1 by buoyancy, and ascends in the partial oxidation portion 26 while turning.
  • the slag generated in the partial oxidation portion 26 is in a molten state.
  • a part of the slag is cooled by the above-mentioned cooling means on the inner peripheral surface of the partial oxidation portion 26 and adheres to the inner peripheral surface, and the other portion is provided inside the slag cooling water tank 29 provided below the partial oxidation portion 26. It is dropped into water W, cooled, and recovered.
  • Gas such as water vapor generated in the partial oxidation unit 26, tar, char and the like are sent out from the partial oxidation unit 26 and rise in the through holes 27 of the thermal decomposition unit 28.
  • the temperature in the partial oxidation portion 26 is adjusted to 1000 ° C. or more, and the pressure is adjusted to 1 MPa or more.
  • the nozzle portion 31 supplies the moisture control coal to the inside of the through hole 27.
  • the moisture control coal is dried by the coal drying and grinding facility 2 and adjusted to have the above-mentioned predetermined moisture amount.
  • the water amount adjustment coal supplied from the nozzle unit 31 generates tar by thermal decomposition.
  • a predetermined amount of water contained in the water amount adjusting coal is heated to become water vapor.
  • the tar and water vapor generated from the water amount adjusting coal supplied from the nozzle 31 are mixed with the tar and water vapor rising from the inside of the partial oxidation portion 26, and carbon monoxide gas and carbon monoxide gas are obtained according to the following chemical reaction formula (6). It is decomposed into hydrogen gas.
  • a part of carbon in the water amount adjustment coal supplied to the thermal decomposition unit 28 reacts with carbon dioxide gas in the thermal decomposition unit 28 and becomes carbon monoxide gas by the following chemical reaction formula (7) .
  • FIG. 5 shows the relationship between the rate of increase of the amount of deposition of tar in the through holes 27 and the amount of water in the moisture control coal.
  • the horizontal axis in FIG. 5 represents the amount of water in the moisture-regulating coal, and the vertical axis represents the rate of increase in the amount of attached tar.
  • Water content control As the water content in the coal increases, the reaction between tar and water vapor is promoted, and the rate of increase in the amount of tar attached decreases. Specifically, if the amount of water in the water amount adjusting coal is smaller than 15%, the amount of adhesion of tar increases and tar adheres in the through holes 27.
  • the water content in the moisture control coal is greater than 15%, tar will not adhere in the through hole 27 and even if tar adheres in the through hole 27 for some reason, the tar will It is decomposed into gas and disappears.
  • the water content in the water amount adjustment coal is 40 It does not exceed%.
  • a high temperature synthesis gas containing hydrogen gas and carbon monoxide gas as main components is transported from the thermal decomposition unit 28 together with char and is supplied to the heat recovery facility 5.
  • the temperature of the steam rises due to the heat exchange between the synthesis gas transported from the thermal decomposition unit 28 and the steam outside. This water vapor is supplied to the aforementioned drying unit 13 and the like for the purpose of drying coal etc.
  • 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 recovery facility 6 recovers the char contained in the synthesis gas.
  • the synthesis gas that has passed through the char recovery facility 6 is supplied to the shift reaction facility 7.
  • the synthesis gas whose components have been adjusted in the shift reaction equipment 7 is supplied to the gas purification equipment 8, and carbon dioxide gas contained in the synthesis gas, a gas containing sulfur as a component, and the like are recovered.
  • the synthesis gas purified by the gas purification facility 8 is supplied to the chemical synthesis facility 9 to produce products such as methane and methanol.
  • the driver reduces the flow rate of the water vapor flowing through the drying unit 13 by a predetermined amount using the flow rate adjustment valve 19 of the drying unit 13.
  • the temperature of the temperature sensor is lowered to T1 and the water content of the moisture control coal obtained by the drying unit 13 is increased from X0 to X1.
  • the water amount adjusting coal having the water amount increased to X1 from the nozzle portion 31 into the through hole 27, more water vapor is generated from the water amount adjusting coal.
  • the reaction between the tar attached to the through hole 27 and the water vapor is promoted by the chemical reaction formula (6), and the attached tar gasifies and disappears.
  • the flow control valve 19 is used to control the flow rate of the steam flowing through the drying unit 13 in order to maintain the reaction speed in the thermal decomposition unit 28 at a predetermined value or more.
  • the flow rate may be increased.
  • the temperature of the temperature sensor may be raised to, for example, T0 or T2, and the water content of the water content adjusting coal may be reduced to X0 or X2.
  • the sub-bituminous coal or the lignite containing 20% or more of moisture by weight ratio is dried by the coal drying and grinding facility 2.
  • a moisture control coal having a predetermined moisture amount larger than the residual moisture amount in the conventional coal gasification system is manufactured.
  • the predetermined amount of water contained in the water amount adjusting coal chemically reacts with the tar generated from the water amount adjusting coal so that the tar does not adhere to the through holes 27 As such, adjust the amount of water in the coal.
  • the moisture control coal and the oxygen-containing gas are supplied at a predetermined ratio without supplying steam from the gasification burner 30 to the storage space 26 a in the partial oxidation unit 26 to burn the moisture control coal.
  • the oxygen-containing gas refers to a gas containing oxygen, and includes not only oxygen gas but also air and oxygen-enriched air.
  • a high concentration oxygen gas having an oxygen content of 85% or more as the oxygen-containing gas.
  • Both carbon and water supplied into the thermal decomposition section 28 are contained in the moisture control coal, and from the moisture control coal, tar and char mainly composed of carbon are generated by thermal decomposition. Further, the moisture in the moisture control coal is heated in the thermal decomposition section 28 to become steam. The tar, char and water vapor immediately after being produced from the moisture control coal are mixed. Therefore, as in the case where they are supplied from separate nozzles, water vapor is supplied to a position away from tar and char, which prevents them from becoming unresponsive.
  • the amount of water in the water amount adjusting coal supplied to the inside of the thermal decomposition portion 28 is adjusted to such an amount that the tar and the steam chemically react with each other by the coal drying and grinding facility 2 and tar does not adhere in the through holes 27 It is done. Therefore, the amount of tar adhering to the through hole 27 does not increase and the through hole 27 is not clogged. Then, the steam supplied from the outside into the thermal decomposition unit 28 from the outside is prevented in the prior art in order to prevent the tar from adhering by reacting the steam, tar and char in the mixed state in the thermal decomposition unit 28 more reliably.
  • the chemical reaction in the thermal decomposition section 28 can be promoted by reducing or eliminating the need.
  • the moisture is supplied to the thermal decomposition section 28 in a state of being contained in the moisture control coal. Therefore, a device for supplying steam to the thermal decomposition unit 28 such as a steam nozzle is not necessary, and the manufacturing cost of the coal gasification system 1 can be reduced.
  • a certain amount of energy is required to heat the coal.
  • coal having a high water content is supplied to the thermal decomposition unit 28 without being dried to the residual water content of coal in a conventional coal gasification system. And, by causing the water in the moisture control coal to react effectively in the thermal decomposition section 28, it is possible to reduce part of the energy that was conventionally required to dry the coal.
  • the amount of water in the water amount adjusting coal is set to 15% or more, the reaction between tar and water vapor in the thermal decomposition portion 28 can be further promoted, and tar can be prevented from adhering to the through holes 27. .
  • tar generated by thermal decomposition of the moisture control coal may be attached.
  • the inventors have determined that the predetermined position D1 above the nozzle portion 31 in the through hole 27 of the thermal decomposition portion 28 (for example, several hundred mm in the upper portion D1 above the nozzle portion 31) It was found that tar was attached intensively at the position). That is, the first pipe 34 of the pressure measuring device 33 is connected to the accommodation space 26 a of the partial oxidation unit 26, and the second pipe 35 is connected to the end 27 a of the upper D 1 of the through hole 27.
  • the pressure measuring device 33 By configuring the pressure measuring device 33 in this manner, it is possible to prevent the pipes 34 and 35 from being clogged by tar and to reliably measure the pressure difference. Since it is known that tar does not easily adhere to the portion D2 lower than the nozzle portion 31 in the through hole 27 of the thermal decomposition portion 28, the first pipe 34 may be connected to this portion.
  • the pressure measurement device 33 is not provided. It is also good. It is not necessary for the water contained in the moisture control coal supplied to the partial oxidation unit 26 and the water contained in the moisture control coal supplied to the thermal decomposition unit 28 to be the same. For example, by preparing two lines of coal drying and crushing and supply system equipment, it is possible to supply moisture-regulating coal having different moisture amounts to the partial oxidation unit 26 and the thermal decomposition unit 28.
  • Water content adjustment coal supplied to the partial oxidation unit 26 will be reduced if the amount of water in the coal is too high, leading to a decrease in efficiency, and water contained in the water amount adjustment coal supplied to the thermal decomposition unit 28 will be large because it leads to adhesion prevention Is preferred.
  • the coal gasification system 41 of the present embodiment has the water content based on the pressure difference measured by the pressure measurement device 33 in addition to the components of the coal gasification system 1 of the first embodiment.
  • the control unit 42 is provided to adjust the amount of water in the adjustment coal.
  • the control unit 42 includes a memory and an arithmetic unit (not shown).
  • the control unit 42 is electrically connected to the pressure measuring device 33, the drying unit 13, and the temperature sensors of the crushing unit 14.
  • the memory as shown in FIG. 7, the relationship between the temperature of the temperature sensor of the crushing unit 14 as shown in FIG. 4 and the amount of water in the moisture control coal after leaving the coal drying and crushing facility 2;
  • a relational expression between the pressure difference measured by the pressure measuring device 33 and the water amount in the water amount adjusting coal necessary to return the pressure difference to a normal value is stored.
  • the arithmetic unit can receive the signal from the pressure measurement device 33 and can control the drying unit 13 based on the above-described relational expression stored in the memory.
  • the arithmetic unit of the control unit 42 detects that the pressure difference has become large by receiving the signal from the pressure measuring device 33. Then, the arithmetic unit calculates X1 of the water content corresponding to P1 of the pressure difference from the relational expression between the pressure difference of the pressure measuring device 33 and the water content adjustment coal shown in FIG. 7 stored in the memory. . Furthermore, the arithmetic unit calculates T1 of the temperature of the temperature sensor corresponding to X1 of the water content from the relational expression between the temperature of the temperature sensor and the water content adjustment in the moisture adjustment coal shown in FIG.
  • the arithmetic unit controls the drying unit 13 to adjust the temperature of the temperature sensor to T1.
  • the water amount adjusting coal whose water amount has increased to X1 is supplied from the nozzle portion 31 of the coal gasification reaction furnace 4 into the thermal decomposition portion 28.
  • the control unit 42 start the above control when the pressure difference measured by the pressure measuring device 33 rises by 10 to 30% compared to that in the normal operation.
  • the arithmetic unit calculates T0 and T2 of the temperature corresponding to P0 and P2 of the pressure difference from both relational expressions, and sets the temperature of the temperature sensor to T0 or T2.
  • the water content of the water control coal may be reduced to X0 or X2 by adjustment.
  • the amount of water supplied to the thermal decomposition unit 28 can be adjusted without requiring an apparatus for supplying water vapor to the thermal decomposition unit 28. Furthermore, when tar adheres to the inside of the through hole 27, the pressure difference measured by the pressure measuring device 33 becomes large. At this time, the chemical reaction between tar and water vapor is further promoted by the arithmetic unit increasing the moisture content of the coal by adjusting the amount of moisture by the coal drying and grinding facility 2, and the tar adhering to the through holes 27 of the thermal decomposition section 28 Can be gasified.
  • the water amount adjusting coal to be supplied to the partial oxidation unit 26 from the amount of steam required for the partial oxidation unit 26 It is conceivable that the amount of water contained in the medium is higher.
  • the coal drying and crushing facility 2 two types of coal, one containing a water content suitable for supplying to the thermal decomposition part 28, and the coal for the partial oxidation part 26 having a water content smaller than that of coal. Manufacture. Then, the two types of coal may be supplied to each of the partial oxidation unit 26 and the thermal decomposition unit 28.
  • the temperature in the partial oxidation unit 26 is 1300 ° C.
  • the water content adjustment coal supplied from the gasification burner 30 into the partial oxidation unit 26 is 18% water content adjustment coal, oxygen-containing gas
  • the flow rates of oxygen gas were 650 (kg / h) and 345 (Nm 3 / h), respectively. Water vapor is not supplied to the partial oxidation unit 26.
  • the drying apparatus used the apparatus which doubles as a grinder shown in FIG. 3, and dried and grind
  • tar is not attached to the through-hole 27 when 150 kg / h of water-regulating coal with a water content of 18% is supplied from the nozzle portion 31 to the thermal decomposition portion 28 and steam is not supplied. I found that.
  • tar can be prevented from adhering and stable operation can be performed without installing devices such as a steam nozzle and a steam supply pump.
  • the equipment as a whole could be made into a compact equipment configuration.
  • the pressure difference between the inside of the partial oxidation unit 26 and the thermal decomposition unit 28 was measured by the first pipe 34 and the second pipe 35 using the above-described coal gasification system 1. Then, coal 606 (kg / h) having a water content of 10% and oxygen-containing gas (oxygen gas in the present embodiment) 330 (Nm 3 / h) were supplied into the partial oxidation section 26. In addition, 136 (kg / h) of water content adjusting coal having a water content of 12% was supplied from the nozzle portion 31 into the thermal decomposition portion 28 and operated. In addition, the drying apparatus used the apparatus which served as the crusher of FIG.
  • the amount of water vapor in the upper reaction container can be adjusted without requiring an apparatus for supplying water vapor to the upper reaction container.
  • coal gasification system coal drying and pulverizing equipment (drying device) 4 coal gasification reactor 26 partial oxidation part (lower reaction vessel) 26a accommodation space 27 through hole 28 thermal decomposition part (upper reaction vessel) 28a diameter reduction Unit 30 Gasification burner (burner unit) 33 Pressure measuring device (pressure measurement unit) 42 Control unit D Vertical direction

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

L'invention concerne un système de gazéification de charbon et une méthode de gazéification de charbon, comprenant un appareil de séchage qui transforme du charbon sub-bitumineux ou du lignite en charbon à humidité régulée par séchage jusqu'à ce qu'il contienne une teneur en humidité spécifiée ; et une chaudière de réaction de gazéification du charbon qui produit au moins de l'hydrogène et du monoxyde de carbone en brûlant le charbon à humidité régulée. La teneur en humidité spécifiée est fixée à un niveau tel que quand la vapeur d'eau émise depuis le charbon à humidité régulée et le goudron réagissent chimiquement, le goudron ne colle pas dans les trous traversants.
PCT/JP2011/057482 2010-04-16 2011-03-25 Système de gazéification de charbon et méthode de gazéification de charbon WO2011129192A1 (fr)

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CN201180018831.6A CN102892869B (zh) 2010-04-16 2011-03-25 煤气化系统及煤气化方法
JP2012510610A JP5450799B2 (ja) 2010-04-16 2011-03-25 石炭ガス化システムおよび石炭ガス化方法
AU2011241630A AU2011241630B2 (en) 2010-04-16 2011-03-25 Coal gasification system and coal gasification method

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JP2013174182A (ja) * 2012-02-24 2013-09-05 Central Research Institute Of Electric Power Industry 石炭火力発電システム
AU2013251229B2 (en) * 2012-11-08 2016-04-21 Mitsubishi Power, Ltd. Gasification system for solid fuel
JP2018006141A (ja) * 2016-06-30 2018-01-11 三菱重工業株式会社 発電システム
JP2021071241A (ja) * 2019-10-31 2021-05-06 株式会社下瀬微生物研究所 多孔質物質の乾燥装置及びこれを備えた水素製造装置並びに多孔質物質の乾燥方法

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AU2015201766B1 (en) * 2015-04-08 2016-06-09 Mitsubishi Power, Ltd. Gasifying system including a gasifier
CN112029542B (zh) * 2020-08-17 2021-10-26 新奥科技发展有限公司 加氢气化系统及方法

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JP2003027072A (ja) * 2001-07-16 2003-01-29 Nippon Steel Corp 石炭の熱分解ガス化反応生成物による発電方法
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Publication number Priority date Publication date Assignee Title
JP2013174182A (ja) * 2012-02-24 2013-09-05 Central Research Institute Of Electric Power Industry 石炭火力発電システム
AU2013251229B2 (en) * 2012-11-08 2016-04-21 Mitsubishi Power, Ltd. Gasification system for solid fuel
JP2018006141A (ja) * 2016-06-30 2018-01-11 三菱重工業株式会社 発電システム
JP2021071241A (ja) * 2019-10-31 2021-05-06 株式会社下瀬微生物研究所 多孔質物質の乾燥装置及びこれを備えた水素製造装置並びに多孔質物質の乾燥方法
WO2021084942A1 (fr) * 2019-10-31 2021-05-06 株式会社下瀬微生物研究所 Dispositif de séchage pour substance poreuse, dispositif de production d'hydrogène le comprenant, et procédé de séchage de substance poreuse
CN114207371A (zh) * 2019-10-31 2022-03-18 株式会社下濑微生物研究所 多孔质物质的干燥装置、具备该干燥装置的氢制造装置以及多孔质物质的干燥方法
JP7146277B2 (ja) 2019-10-31 2022-10-04 株式会社下瀬微生物研究所 多孔質物質の乾燥装置を備えた水素製造装置、および水素製造方法
CN114207371B (zh) * 2019-10-31 2023-06-27 株式会社下濑微生物研究所 多孔质物质的干燥装置、具备该干燥装置的氢制造装置以及多孔质物质的干燥方法
AU2020376194B2 (en) * 2019-10-31 2023-08-17 Shimose Microbes Laboratory Corporation Drying device for porous substance, hydrogen production device comprising same, and method for drying porous substance

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JP5450799B2 (ja) 2014-03-26
AU2011241630A1 (en) 2012-12-06
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CN102892869A (zh) 2013-01-23
AU2011241630B2 (en) 2013-10-24

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