US20110192079A1 - Method for producing pulverized coal - Google Patents

Method for producing pulverized coal Download PDF

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Publication number
US20110192079A1
US20110192079A1 US12/994,927 US99492709A US2011192079A1 US 20110192079 A1 US20110192079 A1 US 20110192079A1 US 99492709 A US99492709 A US 99492709A US 2011192079 A1 US2011192079 A1 US 2011192079A1
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US
United States
Prior art keywords
drying gas
pulverizer
volume
temperature
oxygen level
Prior art date
Legal status (The legal status 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 status listed.)
Abandoned
Application number
US12/994,927
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English (en)
Inventor
Louis Schmit
Georges Stamatakis
Guy Junk
Claude Junk
Benoît Junk
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Paul Wurth SA
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Paul Wurth SA
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 Paul Wurth SA filed Critical Paul Wurth SA
Assigned to PAUL WURTH S.A. reassignment PAUL WURTH S.A. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: STAMATAKIS, GEORGES, SCHMIT, LOUIS, JUNK, CLAUDE, JUNK, BENOIT
Publication of US20110192079A1 publication Critical patent/US20110192079A1/en
Abandoned legal-status Critical Current

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    • 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
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C23/00—Auxiliary methods or auxiliary devices or accessories specially adapted for crushing or disintegrating not provided for in preceding groups or not specially adapted to apparatus covered by a single preceding group
    • B02C23/04—Safety devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C23/00—Auxiliary methods or auxiliary devices or accessories specially adapted for crushing or disintegrating not provided for in preceding groups or not specially adapted to apparatus covered by a single preceding group
    • B02C23/18—Adding fluid, other than for crushing or disintegrating by fluid energy
    • B02C23/24—Passing gas through crushing or disintegrating zone
    • B02C23/34—Passing gas through crushing or disintegrating zone gas being recirculated to crushing or disintegrating zone
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C21B5/003—Injection of pulverulent coal
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
    • F26B17/101—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis
    • F26B17/103—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis with specific material feeding arrangements, e.g. combined with disintegrating means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
    • F26B21/06—Controlling, e.g. regulating, parameters of gas supply

Definitions

  • the present invention generally relates to a method for the production of pulverized coal, in particular for use in the metallurgical industry.
  • pulverized coal In the metallurgical industry, pulverized coal is generally injected as combustible into blast furnaces. It is important, in order to ensure good functioning of the blast furnace, that the pulverized coal is of good quality, i.e. that the pulverized coal has the right consistence, size and humidity level.
  • the pulverized coal is generally produced in a grinding and drying installation, wherein raw coal is ground in a pulverizer and dried to the right humidity level before the resulting pulverized coal is fed to a hopper for storage or direct use in a blast furnace. It is known to subject the freshly ground coal to a stream of hot gas so as to dry the pulverized coal.
  • the pulverized coal can e.g.
  • the hot gas from the pulverizer to a filter, where the pulverized coal is then separated from the gas and fed to the hopper. Part of the gas is recirculated and heated before it is reintroduced into the pulverizer.
  • the oxygen level in the drying gas is monitored and, if the measured oxygen level is found to be too high, the amount of fresh air introduced into the drying gas in the recirculation line is reduced. This allows lowering the oxygen level in the drying gas.
  • the reduction of the amount of fresh air introduced into the drying gas may not be enough to sufficiently reduce the oxygen level. Indeed, once the amount of fresh air introduced into the drying gas is reduced to zero, i.e. no more fresh air is introduced, the oxygen level may in such circumstances still be too high. In order to avoid any damage to the installation it may then be necessary to shut down the grinding and drying installation. Such a shut down not only leads to a loss of production, but also to extra costs relating to the replacement or conditioning of the drying gas.
  • the present invention proposes a method for producing pulverized coal, the method comprising the steps of:
  • the oxygen level in the drying gas is determined during a grinding cycle wherein heated drying gas is fed through the pulverizer and raw coal is introduced into the pulverizer and if, during the grinding cycle, the determined oxygen level is higher than a predetermined oxygen threshold, water is injected into the heated drying gas before it is fed into the pulverizer, the volume of water injected being calculated so as to reduce the oxygen level below the predetermined oxygen level threshold.
  • the injection of water into the drying gas during the grinding cycle allows increasing the overall volume of the drying gas, thereby reducing the relative oxygen volume. The water injection therefore allows reducing the oxygen level to an acceptable level and thereby avoids any damage to the installation or the need to shut down the grinding and drying installation.
  • the method further comprises injecting, in the recirculation line, fresh air into the drying gas wherein, if the determined oxygen level is higher than the predetermined oxygen level threshold, the volume of fresh air injected into the drying gas is reduced.
  • the method comprises first reducing the volume of fresh air injected into the drying gas, and then, if the volume of fresh air injected reaches zero and the oxygen level is still higher than the predetermined oxygen threshold, injecting water into the heated drying gas before it is fed into the pulverizer, the volume of water injected being calculated so as to reduce the oxygen level below the predetermined oxygen level threshold.
  • the predetermined oxygen threshold is chosen to be between 0 and 14 volume %, preferably between 5 and 12 volume %.
  • the method comprises the further steps of determining an exit temperature of the mixture of drying gas and pulverized coal exiting the pulverizer; and controlling the exit temperature by controlling a volume of water injected into the heated drying gas before feeding it into the pulverizer.
  • the temperature of the drying gas entering the pulverizer can be adjusted rapidly so as to take into account temperature differences occurring due to raw coal with different levels of humidity being introduced into the pulverizer. It is thereby possible to maintain the temperature of the drying gas exiting the pulverizer, hereafter referred to as exit temperature, as constant as possible.
  • the present aspect is of particular advantage during a startup phase of the installation, wherein the method comprises a startup cycle wherein heated drying gas is fed through the pulverizer without introducing raw coal, the exit temperature being kept below a first temperature threshold, and a grinding cycle wherein heated drying gas is fed through the pulverizer and raw coal is introduced into the pulverizer, the exit temperature being kept at a preferred working temperature.
  • the method comprises:
  • drying gas is generally fed through the installation before raw coal is introduced into the pulverizer. This allows the individual components to be heated to the desired working temperature.
  • the drying gas which may be heated to a temperature above the maximum tolerated exit temperature, can be cooled down again so that the temperature downstream of the pulverizer does not exceed the first temperature threshold.
  • the volume of water injected into the heated drying gas can be determined based on the exit temperature. Alternatively, the volume of water injected into the heated drying gas can be determined based on a pressure drop measured across the pulverizer. It is not excluded to use other measurements, alone or in combination, to determine the volume of water to be injected into the heated drying gas.
  • the method comprises the further steps of reducing the heating of the drying gas; and reducing the volume of water injected into the heated drying gas to maintain the desired exit temperature.
  • This allows reducing consumption of energy once the installation is running.
  • the importance of the overheating and subsequent cooling of the drying gas is particularly important during the startup phase of the installation, wherein it allows providing a buffer to compensate for the drop in temperature occurring when the introduction of raw coal is started. Once the installation is running, only smaller temperature drops might occur and the buffer can be reduced.
  • part of the drying gas can be removed as exhaust gas.
  • hot gas can also be injected into the drying gas in the recirculation line.
  • the method may also comprise continuous monitoring of the exit temperature and comparing the measured exit temperature to a maximum temperature, wherein, if the measured exit temperature exceeds the maximum temperature, the volume of water injected into the heated drying gas is increased. This allows using the water injection means used for general process control, to be used for emergency cooling also.
  • FIG. 1 shows a schematic representation of a grinding and drying installation used for carrying out the method according to the present invention.
  • FIG. 1 shows a grinding and drying installation for producing pulverized coal using the method according to the present invention.
  • Such a grinding and drying installation 10 comprises a pulverizer 20 into which raw coal is fed via a conveyor 22 .
  • the raw coal is crushed between internal mobile pieces (not shown) or any other conventional grinding means into a fine powder.
  • a hot drying gas is fed through the pulverizer 20 to dry the pulverized coal.
  • the drying gas enters the pulverizer 20 through a gas inlet 24 .
  • the grinding and drying installation 10 comprises a hot gas generator 26 in which a drying gas can be heated to a predefined temperature.
  • a hot gas generator 26 is powered by a burner 27 , such as e.g. a multiple lance burner.
  • the heated drying gas is carried from the hot gas generator 26 to the pulverizer 20 via a conduit 28 .
  • pulverized coal is entrained.
  • a mixture of pulverized coal and drying gas is carried from the pulverizer 20 , via a conduit 32 , to a filter 34 , where the pulverized coal is again removed from the drying gas and fed to a pulverized coal collector 36 , ready further use.
  • the drying gas exiting the filter 34 is fed to a recirculation line 38 for feeding it back to the hot gas generator 26 .
  • the recirculation line 38 comprises fan means 40 for circulating the drying gas through the installation.
  • the fan means 40 may be located upstream or downstream of a line 42 , e.g. a stack, which is used to extract part of the drying gas from the recirculation line 38 .
  • the recirculation line 38 further comprises gas injection means 44 for injecting fresh air and/or hot gas into the recirculation line 38 .
  • the injected fresh air and/or hot gas is mixed with the recycled drying gas.
  • the injected fresh air allows reducing the due point of the drying gas and the injected hot gas is used to improve the thermal balance of the grinding and drying circuit.
  • the installation 10 comprises water injection means 46 arranged downstream of the hot gas generator 26 and upstream of the pulverizer 20 .
  • the importance of the water injection means 46 will become clear in the description herebelow.
  • the water injection means 46 helps to regulate the dew point of the drying gas by regulating the oxygen level therein.
  • part of the drying gas is extracted via the line 42 and fresh air may be injected via the gas injection means 44 .
  • the oxygen level is monitored for safety reasons by means of an oxygen sensor 45 and, if the oxygen level is found to be too high, the gas injection means 44 is instructed to reduce the amount of fresh air introduced into the dying gas.
  • a problem however occurs when the gas injection means 44 reaches its shut-off point, i.e. when the gas injection means 44 is completely turned off and no fresh air is injected into the dying gas. If the oxygen level is then still found to be too high, the volume of fresh air injected into the dying gas cannot be further reduced and a shutdown of the installation becomes necessary.
  • the oxygen level in the drying gas can be reduced by injecting water into the drying gas by means of the water injection means 46 .
  • the water injection means 46 can be instructed to increase the volume of water injected into the drying gas, thereby reducing the oxygen level downstream of the filter 34 .
  • the oxygen level is first reduced by the conventional method of reducing the volume of fresh air injected into the dying gas by the gas injection means 44 and if this is not sufficient, the oxygen level is then further reduced by increasing the volume of water injected into the drying gas by the water injection means 46 .
  • Another function of the water injection means 46 may be to help regulate the temperature of the drying gas at the exit of the pulverizer 20 .
  • the drying gas is heated to a predefined temperature in the hot gas generator 26 and fed through the pulverizer 20 .
  • the temperature of the drying gas is reduced in the pulverizer 20 as the heat from the drying gas is used to dry the pulverized coal.
  • the level of humidity of the raw coal determines the temperature loss of the drying gas.
  • the temperature of the mixture of pulverized coal and drying gas exiting the pulverizer 20 hereafter referred to as the exit temperature, is monitored, e.g. by means of a temperature sensor 48 .
  • the temperature of the drying gas entering the pulverizer needs to be controlled, which is generally achieved by controlling the output power of the burner 27 of the hot gas generator 26 .
  • this process has a relatively slow response time, meaning that once the installation has determined that the exit temperature is too high or too low and the burner 27 has been made to react in consequence, some time passes before the exit temperature reaches the correct exit temperature again.
  • the response time is particularly important during a startup phase of the installation. Indeed, initially, heated drying gas is fed through the installation before the raw coal is introduced. This allows the installation to heat up and reach the ideal working conditions. When, after a certain time, raw coal is then introduced into the pulverizer 20 , the exit temperature suddenly drops well below the desired exit temperature. Conventionally, the burner 27 then reacts by further heating the drying gas so as to reach the desired exit temperature. The desired exit temperature is then however only obtained after a long delay and any pulverized coal obtained in the meantime may have to be discarded because it has not been sufficiently dried. Indeed, during a transition period wherein the exit temperature is too low, unusable coal slurry is generally obtained instead of dried pulverized coal.
  • the burner 27 is set to heat the drying gas well above the desired exit temperature.
  • the heated drying gas is then subjected to controlled cooling by injecting water into the heated drying gas through the water injection means 46 , whereby the drying gas is cooled so that the desired exit temperature can be achieved.
  • the exit temperature suddenly drops well below the desired exit temperature.
  • the amount of water injected into the drying gas by the water injection means 46 is reduced.
  • the heated drying gas is hence cooled less and the desired exit temperature can be kept stable.
  • the reaction time of this procedure is considerably lower than the conventional one, thereby considerably reducing or avoiding a transition period wherein the exit temperature is too low and the production of unusable coal slurry.
  • this method shows its most dramatic advantages during the startup phase, i.e. during a transition period shortly after raw coal is initially introduced into the pulverizer.
  • the present method is however also advantageous during normal operation of the installation.
  • the exit temperature can be quickly brought back to the desired exit temperature should a sudden drop in temperature occur.
  • the water injection means 46 is also used for an emergency cooling.
  • the method may comprise continuous monitoring of the exit temperature and comparing the measured exit temperature to a maximum temperature. When the measured exit temperature exceeds the maximum temperature, the water injection means 46 is instructed to increasing the volume of water injected into the heated drying gas, thereby reducing the temperature of the drying gas entering the pulverizer 20 and consequently also the temperature of the drying gas exiting the pulverizer 20 .

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Food Science & Technology (AREA)
  • General Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Manufacturing & Machinery (AREA)
  • Metallurgy (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Drying Of Solid Materials (AREA)
  • Disintegrating Or Milling (AREA)
  • Coke Industry (AREA)
US12/994,927 2008-06-02 2009-06-02 Method for producing pulverized coal Abandoned US20110192079A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
LU91451 2008-06-02
LU91451A LU91451B1 (en) 2008-06-02 2008-06-02 Method for producing pulverized coal
PCT/EP2009/056763 WO2009147153A1 (en) 2008-06-02 2009-06-02 Method for producing pulverized coal

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US20110192079A1 true US20110192079A1 (en) 2011-08-11

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US (1) US20110192079A1 (de)
EP (1) EP2300562B1 (de)
JP (1) JP5758800B2 (de)
KR (1) KR101590920B1 (de)
CN (1) CN102046758A (de)
AU (1) AU2009253965B2 (de)
BR (1) BRPI0913362B1 (de)
CA (1) CA2725276C (de)
LU (1) LU91451B1 (de)
RU (1) RU2502780C2 (de)
TW (1) TWI475105B (de)
UA (1) UA104863C2 (de)
WO (1) WO2009147153A1 (de)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140263772A1 (en) * 2013-03-15 2014-09-18 Alstom Technology Ltd Pulverizer monitoring
CN107051689A (zh) * 2017-01-16 2017-08-18 中国电力工程顾问集团西南电力设计院有限公司 一种石灰石干磨制备布置结构
US20230002692A1 (en) * 2021-06-30 2023-01-05 Kunming University Of Science And Technology System for combined production of yellow phosphorus and syngas
US20230002693A1 (en) * 2021-06-30 2023-01-05 Kunming University Of Science And Technology Phosphorus coal gasification reaction device for combined production of yellow phosphorus and syngas

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CA2782436C (en) 2009-12-04 2018-05-22 Barrick Gold Corporation Separation of copper minerals from pyrite using air-metabisulfite treatment
US8349036B2 (en) 2010-01-06 2013-01-08 General Electric Company Systems and method for heating and drying solid feedstock in a gasification system
JP5949414B2 (ja) * 2012-10-05 2016-07-06 新日鐵住金株式会社 粉砕プラント排ガス制御装置、粉砕プラント排ガス制御方法、及びコンピュータプログラム
KR101522781B1 (ko) * 2013-10-17 2015-05-26 주식회사 포스코 미분탄을 이용한 코크스용 점결탄의 제조방법 및 이를 이용한 코크스 제조방법
CN104841544B (zh) * 2015-06-02 2017-08-11 天华化工机械及自动化研究设计院有限公司 一种氮气密闭循环pva制粉方法
KR101759329B1 (ko) * 2015-12-23 2017-07-18 주식회사 포스코 코크스 오븐 가스의 증량시스템 및 그 증량방법
CN107488770A (zh) * 2017-10-17 2017-12-19 中冶赛迪工程技术股份有限公司 一种高炉喷煤制粉系统加湿工艺及装置
RU2771032C1 (ru) * 2021-08-13 2022-04-25 Федеральное автономное учреждение "25 Государственный научно-исследовательский институт химмотологии Министерства обороны Российской Федерации" Технологическая линия получения мелкодисперсного угольного топлива

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EP0467375A1 (de) * 1990-07-20 1992-01-22 Kawasaki Steel Corporation Trockeneinrichtung für in einen Hochofen einzublasenden Kohlenstaub

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GB1467744A (en) * 1974-08-16 1977-03-23 Coaltek Ass Method of maintaining coal heating equipment at standby temperature
US4280283A (en) * 1978-12-02 1981-07-28 Klockner-Humboldt-Deutz Ag Method and device for the operation of a hot gas generator within a dryer
US4244529A (en) * 1979-05-07 1981-01-13 The Cleveland Cliffs Iron Company Inerting of pulverizing mills for combustible materials
US4498632A (en) * 1981-07-22 1985-02-12 Rheinische Braunkohlenwerke Ag Process for grind-drying wet solid fuel
EP0467375A1 (de) * 1990-07-20 1992-01-22 Kawasaki Steel Corporation Trockeneinrichtung für in einen Hochofen einzublasenden Kohlenstaub

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140263772A1 (en) * 2013-03-15 2014-09-18 Alstom Technology Ltd Pulverizer monitoring
US9494319B2 (en) * 2013-03-15 2016-11-15 General Electric Technology Gmbh Pulverizer monitoring
CN107051689A (zh) * 2017-01-16 2017-08-18 中国电力工程顾问集团西南电力设计院有限公司 一种石灰石干磨制备布置结构
US20230002692A1 (en) * 2021-06-30 2023-01-05 Kunming University Of Science And Technology System for combined production of yellow phosphorus and syngas
US20230002693A1 (en) * 2021-06-30 2023-01-05 Kunming University Of Science And Technology Phosphorus coal gasification reaction device for combined production of yellow phosphorus and syngas

Also Published As

Publication number Publication date
JP2011522916A (ja) 2011-08-04
CN102046758A (zh) 2011-05-04
CA2725276A1 (en) 2009-12-10
RU2502780C2 (ru) 2013-12-27
JP5758800B2 (ja) 2015-08-05
AU2009253965B2 (en) 2014-12-04
EP2300562B1 (de) 2015-02-25
TW201009064A (en) 2010-03-01
LU91451B1 (en) 2009-12-03
EP2300562A1 (de) 2011-03-30
UA104863C2 (uk) 2014-03-25
CA2725276C (en) 2016-02-09
BRPI0913362A2 (pt) 2015-11-24
KR20110016463A (ko) 2011-02-17
TWI475105B (zh) 2015-03-01
AU2009253965A1 (en) 2009-12-10
BRPI0913362B1 (pt) 2018-01-23
RU2010154520A (ru) 2012-07-20
KR101590920B1 (ko) 2016-02-02
WO2009147153A1 (en) 2009-12-10

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AS Assignment

Owner name: PAUL WURTH S.A., LUXEMBOURG

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SCHMIT, LOUIS;STAMATAKIS, GEORGES;JUNK, CLAUDE;AND OTHERS;SIGNING DATES FROM 20110331 TO 20110418;REEL/FRAME:026181/0445

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION