WO2013125608A1 - 改質石炭製造設備 - Google Patents

改質石炭製造設備 Download PDF

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Publication number
WO2013125608A1
WO2013125608A1 PCT/JP2013/054251 JP2013054251W WO2013125608A1 WO 2013125608 A1 WO2013125608 A1 WO 2013125608A1 JP 2013054251 W JP2013054251 W JP 2013054251W WO 2013125608 A1 WO2013125608 A1 WO 2013125608A1
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WO
WIPO (PCT)
Prior art keywords
gas
dry distillation
coal
heated
waste heat
Prior art date
Application number
PCT/JP2013/054251
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English (en)
French (fr)
Japanese (ja)
Inventor
慶一 中川
大本　節男
佐藤　文昭
佐藤　淳
Original Assignee
三菱重工業株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 三菱重工業株式会社 filed Critical 三菱重工業株式会社
Priority to CN201380005984.6A priority Critical patent/CN104066823B/zh
Priority to IN5934DEN2014 priority patent/IN2014DN05934A/en
Priority to AU2013223200A priority patent/AU2013223200B2/en
Priority to DE112013001130.1T priority patent/DE112013001130T5/de
Priority to US14/373,542 priority patent/US20140373436A1/en
Publication of WO2013125608A1 publication Critical patent/WO2013125608A1/ja

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
    • C10L5/26—After-treatment of the shaped fuels, e.g. briquettes
    • C10L5/28—Heating the shaped fuels, e.g. briquettes; Coking the binders
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/30—Other processes in rotary ovens or retorts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a modified coal production facility, and is particularly useful when applied to reforming low-grade coal (poor coal) having a high moisture content such as lignite and subbituminous coal.
  • Low-grade coal with a high moisture content such as lignite and sub-bituminous coal has a low calorific value per unit weight, so it can be heated and dried to produce a calorific value per unit weight. To increase.
  • modified coal production equipment for reforming such low-grade coal examples include, for example, an indirect heating type dry distillation apparatus that indirectly heats low-grade coal with a heating gas and dry distillation generated in the dry distillation apparatus.
  • an indirect heating type dry distillation apparatus that indirectly heats low-grade coal with a heating gas and dry distillation generated in the dry distillation apparatus.
  • the above-mentioned dry distillation gas is composed of a low boiling point component, but is accompanied by a high boiling point component tar (dry distillation oil) in order to treat the low-grade coal at a relatively high temperature.
  • tar dry distillation oil
  • the dry distillation gas is cooled, the tar adheres to the wall surface of a duct or the like through which the dry distillation gas flows. As the amount of tar attached increases, problems such as blocking the duct may occur, and various techniques for removing the tar have been developed.
  • Patent Document 1 air is diluted with water vapor or an inert gas to adjust the oxygen concentration to 3% to 21% by volume, and the gas is adjusted to a temperature of 350 ° C. to 500 ° C.
  • a decoking method for burning and removing the coke is disclosed.
  • Patent Document 2 by supplying an oxygen-containing gas into the inner cylinder of the external heat kiln, organic carbides and combustible gas in the processed product generated by thermal decomposition are combusted, whereby heat is generated.
  • a method for thermally decomposing a processed product using an external heat kiln in which the temperature of the cracked gas is increased to prevent liquefaction or solidification thereof.
  • JP 2004-3738 A see, for example, paragraphs [0011], [0014], [0015], etc.
  • the tar generated during operation can be burned to prevent the tar from adhering to the dry distillation gas supply pipe.
  • the oxygen concentration adjusting gas is to be produced from air or an inert gas (nitrogen or water vapor)
  • a device for that purpose is required, and the production cost of the reformed coal increases due to this device.
  • the oxygen concentration adjusting gas must be heated in advance, and additional energy is required. That is, tar could not be removed efficiently.
  • the present invention has been made to solve the above-described problems, and provides a modified coal production facility that can efficiently remove tar without reducing the production amount of the modified coal.
  • the purpose is that.
  • the reformed coal production facility that solves the above-mentioned problems includes a drying means for drying coal, an indirect heating type dry distillation means for indirectly heating the dried coal with a heating gas, and dry distillation.
  • a reformed coal production facility comprising a cooling means for cooling the coal, the heated gas generating means for generating the heated gas, and the dry distillation generated by the indirectly heated dry distillation means to the heated gas generating means
  • a waste heat gas generating means for supplying a gas, a part of the heated gas generated by the heated gas generating means, and exchanging heat of the heated gas to generate a waste heat gas;
  • a waste gas and a mixed gas supply means for supplying the dry distillation gas supply means with a low-temperature heating gas obtained by indirectly heating the coal with the heated gas in the indirectly heated dry distillation means.
  • the reformed coal production facility according to the second invention that solves the above-described problem is the modified coal production facility according to the first invention described above, and is provided in the dry distillation gas supply means to measure the gas temperature. Further comprising a gas temperature measuring means, wherein the mixed gas supply means adjusts the flow rate of the waste heat gas and the low temperature heating gas supplied to the dry distillation gas supply means, and the gas flow rate adjustment means, And control means for controlling based on the gas temperature measured by the gas temperature measuring means.
  • the low-temperature heating gas and the waste heat gas can be supplied to the dry distillation gas supply means.
  • the oxygen concentration is about 1 to 2% due to the low temperature heating gas and the waste heat gas.
  • the tar is oxidatively decomposed.
  • the tar is lightened and the tar is prevented from adhering to the wall surface of the duct or the like constituting the dry distillation gas supply means.
  • the temperature of the dry distillation gas is increased, and the tar is prevented from adhering to the wall surface of the duct or the like constituting the dry distillation gas supply means.
  • Tar can be oxidatively decomposed without stopping the apparatus, and the operating rate of the equipment can be improved as compared with equipment for stopping the apparatus and oxidatively decomposing tar. That is, tar can be efficiently removed.
  • the temperature of the dry distillation gas, the low-temperature heating gas and the waste heat gas is almost the same, and preheating of the low-temperature heating gas and the waste heat gas is unnecessary, which saves energy.
  • low-grade coal 1 such as lignite or bituminous coal is supplied to a drying device 111 which is a drying means for drying the low-grade coal 1 by a hopper or the like (not shown).
  • the delivery port of the drying device 111 communicates with a receiving port 122a of the carbonization device 121 for carbonizing the dry coal 2.
  • the outlet 122 b of the carbonization device 121 communicates with an inlet of a cooling device 131 that is a cooling means for cooling the carbonized coal 3.
  • the dry distillation apparatus 121 includes an inner cylinder 122 and an outer cylinder 123 that covers the inner cylinder 122.
  • the heating gas 11 described later is supplied to the outer cylinder 123.
  • the dry coal 2 supplied in the inner cylinder 122 is indirectly heated and dry-distilled, and the dry-distilled coal 3 is produced
  • the dry distillation apparatus 121 is an indirect heating type apparatus in which the high-temperature gas (heating gas) serving as a heat source and the low-grade coal 1 are not in direct contact, for example, an external heating kiln or the like, and constitutes an indirect heating type dry distillation means. .
  • the gas discharge port of the inner cylinder 122 of the carbonization apparatus 121 communicates with the gas inlet of the combustion furnace 124 via the carbonization gas supply pipe 101.
  • generated by dry distillation is supplied to the gas inlet of the combustion furnace 124.
  • FIG. A fuel (not shown) such as natural gas is also supplied to the gas receiving port of the combustion furnace 124.
  • fuel such as the dry distillation gas 14 and natural gas burns to generate the heated gas 11. That is, the combustion furnace 124 serves as a heated gas generation unit.
  • the gas discharge port of the combustion furnace 124 communicates with the gas inlet of the outer cylinder 123 of the dry distillation apparatus 121 via the heated gas supply pipe 51.
  • the heated gas supply pipe 51 communicates with the gas inlet of the steam generator 125 via the heated gas branch pipe 53.
  • the steam generator 125 serves as a waste heat gas generating unit that generates heat and heat 13 by generating heat by the heat gas 11 exchanging heat with water.
  • the gas discharge port of the steam generator 125 communicates with an exhaust pipe 52 described later via a waste heat gas supply pipe 54.
  • the gas discharge port of the outer cylinder 123 of the dry distillation apparatus 121 is an exhaust gas purification means for purifying the low temperature heating gas 12 generated by heating the inner cylinder 122 and the waste heat gas 13 through the exhaust pipe 52. It communicates with a gas inlet of an exhaust gas treatment device 127. The low-temperature heating gas 12 and the waste heat gas 13 are purified by the exhaust gas processor 127 and discharged out of the system.
  • the exhaust pipe 52 communicates with the gas receiving port of the blower 126 via the mixed gas supply pipe 55.
  • the gas outlet of the blower 126 communicates with the gas inlet of the combustion furnace 124 through the mixed gas supply pipe 56.
  • the mixed gas supply pipe 56 communicates with the mixed gas branch pipe 102.
  • the mixed gas branch pipe 102 communicates with the mixed gas communication pipe 104 via the flow rate adjusting valve 103.
  • the mixed gas communication pipe 104 communicates with the dry distillation gas supply pipe 101.
  • the dry distillation gas supply pipe 101 is provided with a gas temperature measuring device 105 which is a gas temperature measuring means for measuring the gas temperature in the pipe.
  • the gas temperature measuring device 105 is connected to the control device 106 so as to be able to transmit the measured gas temperature to the control device 106 which is a control means for controlling the valve opening degree of the flow rate adjusting valve 103.
  • the exhaust pipe 52, the waste heat gas supply pipe 54, the mixed gas supply pipe 55, the blower 126, the mixed gas supply pipe 56, the mixed gas branch pipe 102, the flow rate adjusting valve 103, the mixed gas communication pipe 104 and the like are mixed gas supply means. I am doing.
  • the hopper quantitatively transfers the low-grade coal 1 at room temperature to the drying device 111.
  • the low-grade coal 1 supplied to the drying device 111 is heated to about 200 ° C. by drying combustion gas (about 150 to 300 ° C.) from a drying combustor (not shown) to remove moisture.
  • the charcoal 2 is transferred into the inner cylinder 122 of the dry distillation apparatus 121.
  • the dry coal 2 transferred to the carbonization device 121 is indirectly heated and dry-distilled with the heated gas 11 (gas temperature: about 1050 ° C., oxygen concentration: about 2-3%) from the combustion furnace 124, Components such as the dry distillation gas 14 containing gaseous tar are removed to form the dry distillation coal 3 and fed to the cooling device 131.
  • the dry-distilled coal 3 fed to the cooling device 131 becomes the reformed coal 4 by being cooled to about 50 ° C.
  • the heated gas 11 (gas temperature: about 1050 ° C., oxygen concentration: about 2-3%) generated in the combustion furnace 124 is fed to the outer cylinder 123 of the dry distillation apparatus 121 through the heated gas feed pipe 51.
  • the heating gas 11 used for heating the inner cylinder 122 in the outer cylinder 123 becomes a low-temperature heating gas 12 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%).
  • the low-temperature heating gas 12 is supplied to the exhaust pipe 52.
  • the heated gas 11 is fed to the steam generator 125 via the heated gas feed pipe 51 and the heated gas branch pipe 53.
  • the heated gas 11 used to generate water vapor by the steam generator 125 becomes the waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%).
  • the waste heat gas 13 is supplied to the exhaust pipe 52 through the waste heat gas supply pipe 54.
  • a part of the low-temperature heating gas 12 and the waste heat gas 13 is supplied to the exhaust gas treatment device 127.
  • the low-temperature heating gas 12 and the waste heat gas 13 are purified by the exhaust gas processor 127 and discharged out of the system.
  • the remainder of the low-temperature heating gas 12 and the waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%) is fed to the blower 126 via the mixed gas feed pipe 55.
  • a part of the low-temperature heating gas 12 and the waste heat gas 13 fed to the blower 126 is supplied to the combustion furnace 124 through the mixed gas supply pipe 56. Further, the remainder of the low-temperature heating gas 12 and waste heat gas 13 (gas temperature: about 350 ° C., oxygen concentration: about 2-3%) fed to the blower 126 is mixed gas branch pipe 102, flow rate adjustment valve 103, It is supplied to the dry distillation gas supply pipe 101 through the mixed gas communication pipe 104.
  • the valve opening degree of the flow rate adjusting valve 103 is controlled by the control device 106 based on the gas temperature measured by the gas temperature measuring device 105. For example, when the gas temperature measured by the gas temperature measuring instrument 105 reaches 400 ° C. or higher, the control device 106 opens the flow rate adjusting valve 103 and adjusts the opening to increase, and when the gas temperature becomes higher than 550 ° C.
  • the flow rate adjustment valve 103 is adjusted to be throttled.
  • a mixed gas in which the low-temperature heating gas 12 and the waste heat gas 13 (oxygen concentration: about 2 to 3%) and the dry distillation gas 14 gas temperature: about 400 ° C., oxygen concentration: 0%
  • the oxygen concentration in the gas is adjusted to about 1 to 2%.
  • gaseous tar dry distillation oil
  • adhesion of the tar to the dry distillation gas supply pipe 101 can be prevented. That is, by adjusting the supply amounts of the low-temperature heating gas 12 and the waste heat gas 13 to the dry distillation gas supply pipe 101 based on the gas temperature in the dry distillation gas supply pipe 101, tar is formed on the wall surface in the dry distillation gas supply pipe 101. Decoking is performed at the timing of adhesion, and tar can be efficiently removed.
  • the low-temperature heating gas 12 and the waste heat gas 13 are supplied into the dry distillation gas supply pipe 101, whereby the gases 12, 13 in the dry distillation gas supply pipe 101 are supplied.
  • 14 is adjusted to about 1-2%, and tar (dry distillation oil) contained in the dry distillation gas 14 is oxidatively decomposed (decoking) to lighten the tar, thereby reducing the dry distillation gas supply pipe 101.
  • the tar can be prevented from adhering to the surface.
  • the temperature of the dry distillation gas 14 is increased, and the attachment of the dry distillation oil to the wall surface of the dry distillation gas supply pipe 101 and the like is prevented.
  • the temperature of the dry distillation gas 14, the low-temperature heating gas 12 and the waste heat gas 13 is substantially the same, and preheating of the low-temperature heating gas 12 and the waste heat gas 13 is not necessary, thereby saving energy.
  • tar can be decoked without stopping the apparatus, and the operating rate of the equipment can be improved as compared with equipment for stopping the apparatus and decoking tar. That is, tar can be efficiently removed.
  • the modified coal production facility according to the present invention can efficiently remove tar without reducing the production amount of the modified coal, it can be used extremely beneficially in various industries.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Materials Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Geology (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Coke Industry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
PCT/JP2013/054251 2012-02-24 2013-02-21 改質石炭製造設備 WO2013125608A1 (ja)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CN201380005984.6A CN104066823B (zh) 2012-02-24 2013-02-21 改性煤制造设备
IN5934DEN2014 IN2014DN05934A (zh) 2012-02-24 2013-02-21
AU2013223200A AU2013223200B2 (en) 2012-02-24 2013-02-21 Reformed coal production equipment
DE112013001130.1T DE112013001130T5 (de) 2012-02-24 2013-02-21 Produktionsanlage für refomierte Kohle
US14/373,542 US20140373436A1 (en) 2012-02-24 2013-02-21 Reformed coal production equipment

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2012-038514 2012-02-24
JP2012038514A JP5804971B2 (ja) 2012-02-24 2012-02-24 改質石炭製造設備

Publications (1)

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WO2013125608A1 true WO2013125608A1 (ja) 2013-08-29

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US (1) US20140373436A1 (zh)
JP (1) JP5804971B2 (zh)
CN (1) CN104066823B (zh)
AU (1) AU2013223200B2 (zh)
DE (1) DE112013001130T5 (zh)
IN (1) IN2014DN05934A (zh)
WO (1) WO2013125608A1 (zh)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP5456073B2 (ja) * 2012-01-06 2014-03-26 三菱重工業株式会社 石炭不活性化処理装置
JP5971652B2 (ja) 2012-10-09 2016-08-17 三菱重工業株式会社 石炭不活性化処理装置
JP5536247B1 (ja) 2013-03-04 2014-07-02 三菱重工業株式会社 石炭不活性化処理装置
DE102017125297B4 (de) * 2017-10-27 2021-03-04 ARCUS Technologie GmbH & Co GTL Projekt KG Verfahren zur Herstellung von Koks und/oder Pyrolysegas in einem Drehrohrofen

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5940185B2 (ja) * 1980-03-31 1984-09-28 日本鋼管株式会社 高揮発分非微粘結炭の予備処理方法及び装置
JPS6153390A (ja) * 1984-08-24 1986-03-17 Hitachi Ltd 低品位炭の高品質化装置の温度制御方法
JP2003232507A (ja) * 2002-02-07 2003-08-22 Meidensha Corp 熱分解処理方法
WO2011074279A1 (ja) * 2009-12-18 2011-06-23 三菱重工業株式会社 石炭改質設備

Family Cites Families (5)

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Publication number Priority date Publication date Assignee Title
US4668244A (en) * 1984-08-22 1987-05-26 Hitachi, Ltd. Method and apparatus for upgrading low rank coal
US5279712A (en) * 1991-04-05 1994-01-18 Pasco Nominees Pty Limited Process and apparatus for the pyrolysis of carbonaceous material
ID20131A (id) * 1997-03-31 1998-10-08 Mitsubishi Heavy Ind Ltd Metode dan peralatan pengeringan batu bara, metode untuk penyimpanan lama batu bara yang direformasi dan batu bara yang direformasi yang disimpan lama, dan proses dan sistem untuk produksi batu bara yang direformasi
CN101376813B (zh) * 2007-08-28 2011-12-21 三菱重工业株式会社 高含水有机物的碳化处理方法及其装置
CN101691493B (zh) * 2009-09-15 2013-04-03 北京国电富通科技发展有限责任公司 一种外燃内热式煤干馏炉

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5940185B2 (ja) * 1980-03-31 1984-09-28 日本鋼管株式会社 高揮発分非微粘結炭の予備処理方法及び装置
JPS6153390A (ja) * 1984-08-24 1986-03-17 Hitachi Ltd 低品位炭の高品質化装置の温度制御方法
JP2003232507A (ja) * 2002-02-07 2003-08-22 Meidensha Corp 熱分解処理方法
WO2011074279A1 (ja) * 2009-12-18 2011-06-23 三菱重工業株式会社 石炭改質設備

Also Published As

Publication number Publication date
JP5804971B2 (ja) 2015-11-04
AU2013223200A1 (en) 2014-08-14
CN104066823B (zh) 2016-01-20
IN2014DN05934A (zh) 2015-06-12
CN104066823A (zh) 2014-09-24
AU2013223200B2 (en) 2015-07-16
JP2013173831A (ja) 2013-09-05
US20140373436A1 (en) 2014-12-25
DE112013001130T5 (de) 2014-11-06

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